523647 A7 ______B7 _ 五、發明説明（1) 發明領域 (請先閱讀背面之注意事項再填寫本頁) 本發明係關於一種經由控制觸媒進料速率控制反應速 率之系統和方法。本發明一較佳實例係關於控制連續放熱 程序的方法和系統，例如在一個流化床反應器中進行氣相 聚合反應時生產速率的優化。 發明背景 已有多種方法用於控制反應。其中控制觸媒的進料速 度是較常用的方法。在許多化學反應，如烴類單體的聚合 中，使用觸媒促進化學反應的進行。衆所周知，大部分的 反應對觸媒的使用量較爲敏感，使得可以經由控制觸媒對 反應器的進料速率達到控制反應的目的。 例如，TRIBBLE的美國專利第4，162，894號 揭示一種控制觸媒進料速率的作法和設備。TRIBBLE通過 監控反應器中的反應條件並且產生信號以控制馬達輸送定 量的觸媒進入反應器中。 經濟部智慧財產局員工消費合作社印製 T R I B B L E揭示出觸媒可以根據冷卻劑溫差（△ T ) 控制器控制觸媒進量。 AGARWAL的美國專利第4，669，473號揭示〜 種乙烯聚合反應器的控制系統。AGARWAL揭示出進入進料 管的觸媒的量是經由進料管中原料濃度或進料管中的原料 流的函數來控制的。AGARWAL揭示出控制設備可經由最大 化反應器溫度、觸媒流動速率、冷卻劑流動速率、反應器 出口溫度和最大化反應器中的聚合來達到優化其製程的自 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） 77] 523647 A7 B7 五、發明説明（2) (請先閲讀背面之注意事項再填寫本頁) 的。AGARWAL進一步揭示出其中的觸媒進料設備是根據反 應器總進料流量、反應器最高溫度和所需產品品質來實現 其控制。AGARWAL同時揭示多點控制觸媒的添加。 MAUL EON等人的美國專利第4 ，8 1 8 ，3 7 2號揭 示一種帶有反應溫度控制的用於烴給料的催化裂化之裝置 。MAULEON等揭示一種由溫度感測器控制的閥，用於調節 再生觸媒的注射速率。 GROSS等人的美國專利第4，093，537和 4 ，2 1 1 ，6 3 6號闡述一種液態催化控制部件。 GROSS等人的專利揭示一種根據反應器溫度調節觸媒流動 速率的方法。GROSS等人的專利同時揭示一種根據再生器 溫度控制再生觸媒的循環比率用以補償觸媒損失的方法。 經濟部智慧財產局員工消費合作社印製 GROSS等人的美國專利第4，2 8 2，0 8 4號揭示 一種催化裂化製程。GROSS等人揭示一種用於控制觸媒總 量的計算方法，例如，經由控制觸媒的再生，在該方法中 控制所需的氧化活性得到合適的C〇2 / C〇比。GROSS 等人揭示將進料和觸媒活性的資料登錄到優化製程的執行 優化器中。GROSS等人揭示一種溫度控制器採集反應物和 反應器溫度的資料控制觸媒的流通速度。 D AS SEL等人的美國專利第5，883，292和 5，9 3 9 ，5 8 2號揭示經由調節反應器內的冷凝以控 制反應的方法。DASSEL等人的專利揭示根據包括反應溫度 在內的多種變數控制觸媒濃度從而控制轉化率和第一露點 -5- 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） 523647 A7 B7 五、發明説明（3) VASSILIOU等人的美國專利第6 ，1 8 3 ，6 9 8號 (請先閲讀背面之注意事項再填寫本頁) 揭示一種設備，該設備經由調節壓力下降速度達到控制一 種烴和一種酸或是其他中間氧化產物的反應速率 。 VASSILIOU等人根據多個變數，如循環流的組成、循環流 的流速，經由調節多種成分的進料速度，包括觸媒，從而 調節壓力下降速度達到控制反應速率的目的。VASSILIOU 等人經由監測反應溫度和調節熱交換器達到合適的反應溫 度。 WEBB等人的美國專利第4，619，901號揭示一 種根據一個由比較實際的和合意的未反應單體濃度得到的 非線性控制信號以調節觸媒的進料速度，從而將聚合反應的 反應溢出物的未反應單體濃度維持於所需濃度。 SCHMIDT等人美國專利第4，6 2 0，0 4 9號揭示 出控制聚丁烯分子量的方法。SCHMIDT等人根據反應器中 的異丁烯濃度調節變數，如觸媒進入反應器的進料速度。 經濟部智慧財產局員工消費合作社印製 MAMEDOV等人的美國專利第5，1 1 6，9 1 5號揭 示一種使用電腦計算孟尼黏度以調節製程參數，如觸媒的 進料速度之方法。MAMEDOV等人同時揭示利用電腦維持反 應器部件之間的溫差得到所需分子量分佈的聚合物。 SWINDELLS等人的美國專利第4，25 1 ，503號 揭示一種用於生產二氧化氯的自動且連續性監控系統。 SWINDELLS等人根據尾氣中的二氧化氯和氯的比値改變觸 媒進料速率。其他的背景參考文獻包括歐洲專利 0906782與美國專利第6，063，877和 -6 - 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） 523647 A7 B7 五、發明説明（4) 4，543，399 號。 ----------41^衣-- (請先閱讀背面之注意事項再填寫本頁) 在氣相聚合反應器中，反應發生於產物例如粒狀的聚 乙烯，和氣態反應物形成的流化床上。觸媒係經注入流化 床中。反應熱經由循環氣流傳遞。該氣流在外部的循環管 道中壓縮冷卻。通入補償進料流以維持所需的反應物濃度 〇 較之於攪拌床反應器和葉輪式反應器，在流化床反應 器中，上游氣流中反應單體和觸媒的均勻分佈對於避免熱 點和聚合物淤塞具有關鍵作用。例如，參閱美國專利第 3，7 9 0，0 3 6號。對於流化床反應器的進一步要求 就是經由反應器的氣體流速必須能夠維持床層的流動狀態 。用以維持流化床的流化懸浮狀態的氣體流速不能經由在 一般條件下僅僅依靠在床底部注入液體來實現。 經濟部智慧財產局員工消費合作社印製 第1圖爲一熟知的氣相反應器系統的示意圖。聚合反 應本質上是高放熱反應，當聚合單體相互結合形成大的複 雜的分子鏈（聚合物）時釋放反應熱。反應熱需要經由對 流從反應位置向外傳輸，否則會造成局部溫度過高，產生 熱點，聚合物結塊或是熔化。如此，溫度控制對於穩定的 反應器操作就顯得很關鍵。而且，在流化床反應器中限制 反應速率的主要因素就是能否將反應熱移出聚合反應區。 聚合反應器採用一種氣態介質分散觸媒，該介質具有 兩種作用，既可以充當反應載體，也可以具有冷卻介質的 作用，將反應熱從生長的聚合物的活化位置移出。在通常 的流化床反應器中採用的一般的散熱方法就是經由在反應 本紙張尺度適用中國國家標準（CNS ) A4規格（210 X 297公釐） 523647 A7 B7____ 五、發明説明（5) 器外部壓縮和冷卻循環氣流。根據冷卻的程度’反應器系 統可以在冷凝模式或乾燥模式下運行。在冷凝模式下’經 由將循環氣冷卻至其露點以下得到兩相流體混合物送回反 應器中，從而提高循環氣的散熱能力。在乾燥運行模式下 ，循環氣冷卻至露點以上後，得到單相的循環氣，也就是 氣相，送回反應器中。 在參照第1圖，該系統的操作模式包括一個反應床進 料溫度的級聯溫度控制器操縱的伺服回路中的回流冷卻水 (C W R )閥，調節進入熱交換器的水溫。該溫度控制過 程中的變數包括一個單回路的直接操縱CWR閥的床層溫 度控制器。除此，操作者可以調節觸媒進料速率維持儘可 能大的反應速率。 在大規模的生產聚合物如聚乙烯所用流化床反應器中 ，經由循環冷卻帶走聚合反應熱的流體的數量必須大於用 於維持流化床的流化狀態和在流化床中混入足量的固體所 需的流體數量。反應器中的流體的流速有一個上限値，防 止過量的固體夾帶。當聚合反應熱（其熱値與聚合反應速 率成正比）等於流體流經反應器吸收的熱量加上其他途徑 的熱損失時’能夠得到穩定的床層溫度。具體的市售氣相 反應器系統有由Union Carbide開發的Unipo|TM系統。 反應位置的熱傳輸是經由採用水作爲冷卻介質的熱交 換器來完成的。反應器中的最大生產速率決定於熱傳輸速 度。發熱速率可由以下公式得到： 發熱速率=QrPrate = MgCp(Tr-Tf) = MwCpw(Twi-Tw。） ---------衣-- (請先閲讀背面之注意事項再填寫本頁) 訂 經濟部智慧財產局員工消費合作社印製 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） -8 - 523647 A7 B7 五、發明説明（6) (請先閲讀背面之注意事項再填寫本頁) 其中是反應熱生成速率（生產聚乙烯時該値約爲 l525Btu/lb . (847kal/kg)); p「ate是聚合物的生成速率；Mg是反應氣（反應物加上惰 性成分）的質量流率；C p是反應介質的平均質量熱容； T r是反應溫度；T f是循環氣進料溫度；μ w是冷卻水 的質量流率；T w ί是熱交換器入口處的水溫；τ w。是熱 交換器出口水溫。 反應系統中加入溫度、壓力、進料位和成分的調節控 制系統。一般而言，操作者爲了最大化一反應器生產速率 ，可以在冷卻極限範圍內手動的調節觸媒進料速率（ R Ρ Μ )。 經濟部智慧財產局員工消費合作社印製 在冷卻極限範圍內最大化反應器生產速率是一個操作 員每日必須面臨的挑戰。由於晝夜溫度的變化和季節溫度 變化，冷卻水的進入溫度呈周期性的變化。觸媒進料器（ c C F )運轉不穩定性引起的隨時可能的進料故障（pickup block down) 和爲了 重新添加觸媒將進料器取下都爲最 大化生產速率提出另一項挑戰。反應氣體熱容量的改變（ 例如經由注射異戊烷）也會改變熱交換器中的冷卻水需求 〇 在不同的聚合過程中使用不同的觸媒，包括齊格勒（ 納塔）觸媒、鉻合金和茂（合）金屬觸媒。反應觸媒可爲 單相的或是多相的，如負載型的齊格勒（納塔）或鉻合金 觸媒。由於各反應的動力學性質相差甚遠’這些觸媒對於 -9- 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） 523647 A7 B7 五、發明説明（7) (請先閱讀背面之注意事項再填寫本頁) 其進料水平的改變的反應時間是不同的。如此，對於操作 者來說，想要一直維持一個最大的而又安全的反應速率是 一個複雜的優化問題。操作者必須預先估計提高觸媒進料 速率所帶來的影響，同時確保反應器在先前所述的約束變 數內得到正常冷卻。對於操作者來說，已有一種趨勢，就 是當需要額外冷卻時，他們通常將系統維持在一個“安全 區” （comfort zone )，該安全區指的是冷卻能力過剩的 區域。 經濟部智慧財產局員工消費合作社印製 如上所述，流化床反應器可以在乾燥模式或冷凝模式 下運行。在乾燥模式下，循環氣流冷卻至露點以上，如此 在循環氣流中只有氣相存在。在冷凝·模式下循環氣流冷卻 至露點以下，在特定條件下形成一種氣液共存的混合物， 如此至少在流化床反應器的入口處一直到其液相揮發或是 進入流化床之間這段區間混合物中的液相夾雜於混合物的 氣相中。冷凝模式可以使時空產率大幅度增長，同時所得 到的產品的性質和質量改變不大，或是不變。經由控制維 持循環熱交換區的出口溫度控制冷凝混合物冷卻至露點以 下的程度，從而達到所需的冷卻程度。很明顯的，如果需 要，還可以在特定條件下將氣體和液體在反應器的入口處 分別注入反應器中形成一種兩相流體。 經由冷凝模式操作，流化床反應器中可以經由將循環 流冷卻至露點以下，再將得到的兩相流體送回反應器中， 用以將流化床反應器維持在一個需要的高於循環流體的露 點以上的溫度，提高聚合物的時空產率。循環流體的冷卻 -10- 本纸張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） 523647 A7 B7 五、發明説明（8) 能力取決於循環流入口和反應器之間的溫差大小以及循環 流體中的冷凝液體的揮發程度。 (請先閲讀背面之注意事項再填寫本頁) 由以上可以得知，控制反應，例如流化床反應的過程 通常是手動操作過程。因此，反應控制通常是煩瑣的、不 準確的和主觀的。雖然已有反應的自動控制系統，仍然有 必要對其進行改善。 發明槪述 在一具體實例中，本發明係關於優化在流化床反應器 中進行的聚合反應的反應速率之系統與方法。本發明亦有 關用於反應自動控制過程中重要變數識別之方法與系統。 經濟部智慧財產局員工消費合作社印製 進一步說，本發明係關於經由根據在反應器操作過程 中可能引起的製程變數的上升或變化來控制觸媒進料速率 ，從而達到控制放熱或吸熱反應過程之方法和系統。如諳 於此藝者所熟知的，這些變數一般稱作製程約束變數。一 般希望經由調整和控制這些製程約束變數使反應器中的化 工過程安全和有效地進行。例如，在放熱反應器中，需要 調節和控制的變數包括：反應器生產速度、有效熱傳輸（ 由冷卻劑的Δ T的函數側得），反應器進料口的露點和冷凝 材料的重量百分比。 全面約束變數操縱控制方案的目的就是調節和控制製 程約束變數·在該處所述的全面約束變數操縱控制方案中 只有一個主要變數，其精確控制是最重要的。每個全面約 束變數操縱控制方案都必須有一個或多個約束變數，也被 -11 - 本紙張尺度適用中國國家標準（CNS ) A4規格（210 X 297公釐） 523647 A7 B7__ 一 五、發明説明（9) (請先閱讀背面之注意事項再填寫本頁) 稱之爲第二變數。在多數和正常運作的情況下，第一控制 變數是一個受控變數。而第二變數一般不在其約束限制以 外，因此無需控制。 在一具體實例中，如此的一種手段一般稱之爲單約束 變數操縱控制。該約束變數操縱控制在控制方案中採用生 產速率作爲第一控制變數。該具體實施例提供了一個根據 某種考慮如供需比，將生產速率控制在一個定値的具體實 例。冷卻水的Δ T、露點或冷凝物的重量百分比和吹掃箱水 位是第二變數或約束變數。該具體實施例中，經由連續協 調的調節和控制主控變數，同時控制和定位第二變數使得 控制方案更加完善’’。 在另一具體實例中，約束變數操縱控制提供了 一個雙 變數或雙系統與約束變數耦合。該雙系統同時監控冷卻水 閥位置和冷卻水Δ T上限。當觸媒改變、外界條件改變或是 某不可測擾動影響反應器工作時（後者通常發生於典型的 氣相聚合反應過程中），雙系統會幫助改善其控制過程的 穩定性。改善後的控制穩定性有助於提高反應速率。 經濟部智慧財產局員工消費合作社印製 在另一具體實例中，本發明係關於一種用於優化反應 速率之反應製程約束變數操縱控制方法，該方法包括：根 據有效熱傳輸和至少一個附加製程約束變數自動連續的控 制觸媒進入反應器的進料速率達到控制反應的目的。此實 施例具有其優點，因爲放熱反應器需要外部冷卻器用於移 除反應產生的熱量。如此的反應器系統裝置有其冷卻能力 限制，並且正如已爲業者所熟知的，這些限制帶來諸多的 本紙張尺度逍用中國國家標準（CNS ) A4規格（210X297公釐） ~Λ0 - 523647 A7 B7 五、發明説明（ΐά (請先閱讀背面之注意事項再填寫本頁) 問題。如果反應溫度過高，根據冷卻器的設計，冷卻器處 於其最大冷卻極限。當處於冷卻極限時，冷卻器的有效熱 傳輸値爲零。該具體實施例能夠使反應器根據其最大生產 速率更加接近有效熱傳輸零點。 在於另一方面中，本發明係關於優化生產速率的一種 反應製程約束變數操縱控制系統，該系統包括：反應器、 向反應器中添加觸媒的觸媒進料器、用於反應器中熱量的 熱傳輸設備、用於測定熱傳輸設備中的有效熱傳輸的有效 熱傳輸感測器、至少一個根據有效熱傳輸量和至少一個額 外的製程約束變數連續自動地控制該觸媒進料器的控制器 〇 於另一方面中，本發明係關於一種優化生產速率的反 應製程約束變數操縱控制的方法，該方法包括：根據有效 熱傳輸連續自動地控制該觸媒進料器；當有效熱傳輸値變 化後超過預設値時發出警告。 經濟部智慧財產局員工消費合作社印製 於另一方面中，本發明係關於一種優化生產速率的反 應製程約束變數操縱控制系統，該系統包括··反應器、向 反應器中添加觸媒的觸媒進料器、用於交換反應器中熱量 的熱傳輸設備、用於測定熱傳輸設備中的有效熱傳輸的有 效熱感測器、至少一個根據有效熱傳輸量連續自動地控制 該觸媒進料器的控制器，其中控制器在有效熱傳輸改變至 超過預設値時發出警告。 於另一方面中，本發明係關於一種用於優化反應速率 的反應製程約束變數操縱控制方法，該方法包括：根據熱 本紙張尺度適用中國國家標準（CNS ) Α4規格（210X297公釐） 523647 A7 B7 五、發明説明（1) 傳裝置閥位置連續自動地控制觸媒進入反應器的速率，從 而控制反應。 (請先閲讀背面之注意事項再填寫本頁) 於另一方面中，本發明係關於一種用於優化反應速率 的反應製程約束變數操縱控制系統，該系統包括：反應器 、向反應器中添加觸媒的觸媒進料器、用於交換反應器中 熱量的熱傳輸設備、一個熱傳輸源、一個用於在熱交換器 和熱傳輸源之間傳送熱傳輸介質的導管、一個用於將至少 部分的熱傳輸介質旁通熱傳輸源使得至少部分的熱傳輸介 質不經過熱傳輸介質再循環進入熱交換器之再循環導管、 一個用於控制旁通熱傳輸介質量和經由熱傳輸源的熱傳輸 介質量的熱傳輸介質閥、一個用於測定熱傳輸介質閥位置 的熱傳輸介質閥感測器、測定熱交換器中的有效熱傳輸値 的有效熱傳輸感測器、至少一個用於控制該觸媒進料器的 控制器、其中熱傳輸介質閥感測器連接於至少一個控制器 上、其中至少一個控制該觸媒進料器的控制器對熱傳輸介 質閥位置回應。 經濟部智慧財產局員工消費合作社印製 於另一方面中，本發明係關於一種用於優化反應速率 的反應製程約束變數操縱控制方法，該方法包括：根據以 下變數連續自動地控制觸媒進入反應器的進料速率控制反 應：有效熱傳輸値、反應器現時生產速率、反應器收集器 中的反應產物的量、反應器循環流中的冷凝物的質量百分 比、其中反應包括用乙烯形成聚乙烯之聚合反應。 於一方面中，該額外反應約束變數包括反應器中的現 時生產速率。 -14- 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） 523647 A7 _ B7_ _ 五、發明説明（〇 於另一方面中，係將現時生產速率與合意生產速率比 較以控制觸媒進料速率。 (請先閲讀背面之注意事項再填寫本頁) 於另一方面中，該額外反應約束變數包括反應器中採 樣器內的反應產物量。 於另一方面中，係將該採樣器內的反應產物量係與所 需的採樣器內的反應產物量比較從而控制觸媒進料速率。 於另一方面中，該額外製程約束變數包括反應器中循 環流的冷凝物重量百分比濃度。 於另一方面中，係將該冷凝物的重量百分比濃度與所 需的循環流的冷凝物的重量百分比濃度相比較。 於另一方面中，該額外製程約束變數包括反應器中循 環流的露點。 於另一方面中，係將該露點與所需露點比較以控制觸 媒進料速率。 於另一方面中，該額外製程約束變數包括循環流中夾 帶的固體量。 經濟部智慧財產局員工消費合作社印製 於另一方面中，係將該循環流中夾帶的固體量與所需 的固體夾帶量比較以控制觸媒進料速率。 於另一方面中，該額外製程約束變數包括粒狀樹脂的 傳送系統速率。 於另一方面中，係將該粒狀樹脂的傳送系統速率與所 需的粒狀樹脂的傳送系統速率値比較以控制觸媒進料速率 〇 於另一方面中，額外製程約束變數包括造粒速率。 -15- 本紙張尺度適用中國國家標準（CNS ) Α4規格（210Χ297公釐） 523647 A7 B7 五、發明説明（ 於另一方面中，係將該造粒速率與所需的造粒速率比 較以控制觸媒進料速率。 (請先閲讀背面之注意事項再填寫本頁) 於另一方面中，該額外製程約束變數包括進料流。 於另一方面中，係將該進料流與所需的進料流比較以 控制觸媒進料速率。 於另一方面中，該根據有效熱傳輸以自動連續控制觸 媒進入反應器的進料速率包括監測熱傳輸介質混合點的Δ T 〇 於另一方面中，該根據有效熱傳輸自動連續控制觸媒 進入反應器的進料速率包括監測熱傳輸介質混合點的Δ T和 監測熱傳輸設備的熱傳輸介質閥的位置。 於另一方面中，該根據有效熱傳輸自動連續控制觸媒 進入反應器的進料速率包括監測熱傳輸介質器的熱傳輸介 質的閥位置。 於另一方面中，該反應器包含一個熱傳輸設備，該熱 傳輸設備包含與反應器進行熱傳輸的熱交換器，以及一個 使熱傳輸介質在熱交換器與熱傳輸源之間形成回路的導管 〇 經濟部智慧財產局員工消費合作社印製 於另一方面中，該熱傳輸設備包含一個用於將至少部 分的熱傳輸介質旁通熱傳輸源使得至少部分的熱傳輸介質 不經過熱傳輸介質源再循環進入熱交換器之再循環導管。 於另一方面中，該再循環導管的設計是在一個混合點 將至少部分的熱傳輸介質在進入熱交換器前與經由熱傳輸 源的熱傳輸介質混合。 -16- 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） 523647 A7 _B7 _ 五、發明説明（ 於另一方面中，一第一溫度感測器在熱傳輸源與混合 點之間測得熱傳輸介質的第一溫度；一第二溫度感測器在 (請先閲讀背面之注意事項再填寫本頁) 混合點與熱交換器之間的位置測得熱傳輸介質的第二溫度 〇 於另一方面中，一控制器將該第二溫度減去該第一溫 度計算得到ΔΤ。 於另一方面中，當Δ Τ變化至高於預設値時，控制器發 出警告。 於另一方面中，該熱傳輸設備包含一個用於控制旁通 熱傳輸源的數量和經由熱傳輸源的熱傳輸介質的量的熱傳 輸介質閥。 於另一方面中，一熱傳輸介質閥感測器測定熱傳輸介 質閥的位置。 於另一方面中，該熱傳輸介質閥的位置與能夠達到的 最大熱傳輸介質閥的位置比較以控制觸媒進料速率，並且 熱傳輸介質閥的位置維持在當改變熱傳輸介質閥位置時能 影響熱交換器的位置。 經濟部智慧財產局員工消費合作社印製 於另一方面中，該方法更包括測定由熱傳輸設備的第 一泵造成的壓力差之做法。 於另一方面中，該方法更包括根據第一泵產生的壓力 差値控制第二泵。 於另一方面中，該反應器包括一流化床。 於另一方面中，該反應包括聚合反應。 於另一方面中，該反應包括乙烯形成聚乙烯的聚合反 -17- 本紙張尺度適用中國國家標準（CNS ) Α4規格（210Χ297公釐） 523647 A7 __B7_ 五、發明説明（4 應。 (請先閲讀背面之注意事項再填寫本頁) 於另一方面中，該系統更包括一種用於控制旁通熱傳 輸源的數量和經由熱傳輸源的熱傳輸介質的量的熱傳輸介 質閥，該系統更包括一種熱傳輸介質閥感測器，用於測定 熱傳輸介質閥的位置，其中熱傳輸介質感測器與至少一個 控制器相連，其中至少一個控制器用於比較熱傳輸介質閥 位置感測器和A T的型號信號從而控制該觸媒進料器。 於另一方面中，該壓力差感測器係連接於一第二泵控 制器的，該控制器根據該第一泵產生的壓力差控制該第二 泵，並且該第二泵控制器與至少一個控制器相同或不同。 於另一方面中，該系統更包括一種循環回路。 於另一方面中，該系統更包括一種用於測定循環回路 中氣體的露點之露點感測器。 於另一方面中，該露點感測器係經連接到至少一控制 器，且其中該至少一控制器係經構造成根據循環回路中氣 體的露點控制該觸媒進料器 經濟部智慧財產局員工消費合作社印製 於另一方面中，該系統更包括一種操作者介面用於接 收一個露點接近値，且至少一個控制器將該露點接近値與 露點比較以控制該觸媒進料器。 * 於另一方面中，該系統更包括一種用於測定循環回路 中的冷凝液重量百分比的冷凝物重量百分比感測器。 於另一方面中，該重量百分比感測器係與至少一個控 制器.相連，其中該控制器係經構造成根據循環回路中的冷 凝物的重量百分比控制該觸媒進料器。 -18- 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） 523647 Α7 Β7 五、發明説明（ιέ (請先閲讀背面之注意事項再填寫本頁) 於另一方面中，該系統更包括一個操作者介面用於接 收允許的冷凝物重量百分比最大値，並且至少一個控制器 經由將該允許的冷凝物重量百分比最大値與冷凝物重量百 分比相比較以控制該觸媒進料器。 於另一方面中，該反應器包括一用於收集反應產物的 收集器。 於另一方面中，該系統更包括一種用於測定收集器中 的反應產物量之反應產物感測器。 於另一方面中，該反應產物感測器與至少一控制器相 連，並且該至少一控制器係經構造成根據收集器中的反應 產物量控制該觸媒進料器。 於另一方面中，該系統更包括一個操作者介面，該介 面係經構造成接收操作者所需的收集器中的反應產物量， 其中至少一個控制器經由比較該値與實際的收集器中的反 應產物的量來控制該觸媒進料器。 於另一方面中，該系統更包括一種用於測定反應器生 產速率的生產速率感測器。 經濟部智慧財產局員工消費合作社印製 於另一方面中，該生產速率感測器與至少一個控制器 相連，且其中該控制器係經構造成根據生產速率控制該觸 媒進料器。 於另一方面中，該系統更包括一個經構造成用於接收 所需生產速率資料的操作員介面，且其中至少一個控制器 係經由比較實際生產速率與所需生產速率來控制該觸媒進 料器。 -19- 本紙張尺度適用中國國家標準（CNS ) Α4規格（210 X297公釐） 523647 Α7 Β7 五、發明説明（ 圖式之簡略說明 (請先閲讀背面之注意事項再填寫本頁) 本發明將經由下面參照所附眾多非限制性圖式的詳細 說明進一步闡述，其中： 第1圖是一種已知的氣相反應器系統示意圖； 第2圖是一種根據本發明得到的氣相反應器系統示意 圖； 第3圖是觸媒進料器的透視圖； 第4圖是觸媒進料器的分解的部分橫截面圖； 第5圖是一個邏輯圖，其中生產速率經由目標生產速 率、冷卻水Δ T，冷卻水閥位置和露點來控制； 第6圖是已經由目標生產速率、目標冷卻水閥位置和 目標露點控制生產的邏輯圖； 第7圖是一個經由生產速率希望値、吹掃箱水位希望 値、冷凝物的最大質量百分比和冷卻水的最大閥位置控制 生產的邏輯圖； 第8圖是R P Μ初始化邏輯的邏輯圖； 經濟部智慧財產局員工消費合作社印製 第9圖是RPM分流器邏輯的邏輯圖； 第1 0圖是給定値處理器的邏輯圖； 第1 1圖是一個RPM防淤塞邏輯圖； 第1 2圖給出了生產速率控制器的操作者介面； 第1 3圖給出了提供給工程師介面的控制屏； 第1 4圖顯示出實例1中的在冷卻約束變數內的生產 速率最大化的結果； 本紙張尺度適用中國國家標準（CNS ) Α4規格（210Χ297公釐） -20 - 523647 Α7 Β7 經濟部智慧財產局員工消費合作社印製 五、發明説明（ιέ 第1 5圖顯示出實例2中的生產速率控制器優化的生 產速率的結果； 第1 6圖顯示出實例3的結果，其中生產速率是反應 器中觸媒量和冷卻水△ Τ的函數； 第1 7圖顯示出比較實例1的結果，其中顯示出調節 露點的潛在重要性。 符號說明 10 反應器 12 反應區 14 反應減速區 16 觸媒進料器 2 1 氣體分析器 2 2 循環管 2 4 熱交換器 2 8 氣體分配板 5 2 計量盤 7 0 冷卻水閥 8 0 第一冷卻水泵 8 2 第二冷卻水泵 10 0 速率控制器 12 0 操作者介面 13 0 觸媒進料器平衡控制器 14 〇 進料器啓動初始化控制邏輯 (請先閲讀背面之注意事項再填寫本頁) 本紙張尺度適用中國國家標準（CNS ) Α4規格（210Χ297公釐） -21 - 523647 Α7 Β7 五、發明説明（ 15 0 R Ρ Μ Ρ I D控制器 (請先閱讀背面之注意事項再填寫本頁) 160 冷卻潛能損失警報器 17 0 C W D T偏離高優先順序警報器 180 CW泵邏輯控制 2 0 0 低信號選擇器 2 12 Ρ I D生產速率控制器 222 ΡID 吹掃箱水位控制器 2 3 2 Ρ I D冷凝物重量百分比控制器 2 4 2 Ρ I D閥位置控制器 2 4 6 Ρ I D冷卻水△ T控制器 260 計算邏輯控制器 262 低信號選擇器 2 9 0 觸媒R Ρ Μ控制器 詳細說明 經濟部智慧財產局員工消費合作社印製 爲了對本發明各具體實例進行說明性的論述，以下經 由實例描述本發明的細節，以提供經認爲最有用且可輕易 地暸解之本發明原理和槪念性方面。因此，超出本發明的 基本暸解所需的細節就不再描述，經由參照圖表進行的說 明使得深諳此藝者能夠很容易的暸解到本發明的多種形式 付諸實用的技藝。 以下描述中的所有的測量的量，除非特別指明，指的 是占給定試樣的重量百分比。如此，例如，3 0 %指的是 占試樣重量比的3 0 %。 -22- 本紙張尺度適用中國國家標準（CNS ) Α4規格（210Χ297公釐） 523647 A7 B7 五、發明説明（2¾ (請先閱讀背面之注意事項再填寫本頁) 除非特別指明，以下所提到的一種化合物或是一種成 分，不光指該化合物或該成分本身，而且還包括其與其他 化合物或成分形成的混合物。 總的看來’本發明係關於一種根據一個或多個約束變 數操縱控制觸媒進料速率之系統與方法。雖然，可以僅經 由一個變數控制觸媒進料速率，多變數系統通常能夠得到 較好的結果。約束變數可以包括反應條件，例如所需的生 產速率、有效熱傳輸（如冷卻水△ T、冷卻水閥位置）、 露點邊界、冷凝物重量百分比、可冷凝物的重量百分比、 產物的移出（如吹掃箱水位），流化程度、夾帶程度、球 狀’粒狀樹脂傳輸速率、和/或原料添加（如原料添加壓 力）。 本發明可以用於控制那些可經由改變觸媒進料速率控 制反應速率的反應。因此，幾乎所有的反應器都可以採用 本發明之方法。本發明同時適用於吸熱和放熱反應過程。 本發明的反應實例包括在流化床中的催化裂化和氣相聚合 〇 經濟部智慧財產局員工消費合作社印製 但是，本發明用於控制流化床放熱聚合反應是一個較 佳的實例。一般而言，流化床製程製備樹脂材料，尤其是 由聚合單體製備聚合物的過程，通常是將一種包含一種或 多種單體的氣流在反應條件和觸媒存在條件下連續的經由 流化床反應器。包含未反應氣態單體的氣流從反應器中連 續的提出，壓縮，冷卻再循環進入反應器中。產物從反應 器中分出。再加入補充的反應單體，如加入循環氣流中。 -23- 本紙張尺度適用中國國家標準（CNS ) A4規格（2丨〇><297公釐） 523647 A7 B7 五、發明説明（2) (請先閲讀背面之注意事項再填寫本頁) 聚合反應是放熱的，因此要求將反應器內的氣流的溫 度在樹脂材料和觸媒的分解溫度以下，而且要使其溫度低 於聚合反應過程中生成的樹脂顆粒的熔化溫度和粘滯溫度 。如此的溫度控制是有必要的，用以防止由於不能以產物 形式連續移出反應器的快速生長的聚合物塊而造成的反應 器堵塞。因此，可以認爲在給定體積的流化床反應器中一 定時間內生成的聚合物的量與從流化床反應器中移出的熱 量直接相關。 以下將更具體的描述一些限制生產速率的約束變數。 本發明是基於對這些約束變數的認識，這些變數包括，但 不限於，所需的生產速率，有效熱傳輸，露點邊界，冷凝 物重量百分比，產物移出（如吹掃箱水位），流化程度， 夾帶程度，造粒器、粒狀樹脂傳輸能力，和/或原料添加 (如原料添加壓力）。如該處所述之“有效熱傳輸”指的 是在給定時間內的有效冷卻能力，可以由冷卻水△ T (大 的△ T對應的是大的有效熱傳輸）和/或冷卻水閥位置決 定。 經濟部智慧財產局員工消費合作社印製 本發明係關於根據一個或多個約束變數的輸入値經由 改變觸媒進料速率控制生產速率的約束變數超越控制方法 和系統。於一方面中，本發明係關於根據所需生產速率、 有效熱傳輸、露點邊界、冷凝物重量百分比、可冷凝物重 量百分比、產物移出（如吹掃箱水位），流化程度，夾帶 程度，造粒器、粒狀樹脂傳輸能力，和/或原料添加（如 原料添加壓力），經由改變觸媒進料速率對反應進行自動 本紙張尺度適用中周國家標準（CNS ) A4規格（210X 297公釐) 「94 一 " 523647 A7 B7 五、發明説明（3 控制。 (請先閲讀背面之注意事項再填寫本頁) 本發明亦是係關於當有效熱傳輸突然變化時引發警報 之系統與方法。 而且，本發明係關於控制第二泵之方法與系統，合適 的控制第二泵可以使得生產速率的自動控制最佳運轉，避 免反應失控。 爲了更佳瞭解本發明的控制系統及方法之優點，以下 列出氣相聚合反應之非限制性實例。爲了更佳暸解本發明 關於氣相聚合反應之自動控制之系統與方法，需要大致的 對流化床氣相聚合反應有所暸解。 經濟部智慧財產局員工消費合作社印製 雖然，本發明之流化床反應器並不局限於某些特定的 反應器’如上所述，本發明之反應器必須可以運行於乾燥 f吴式和冷凝模式。一般而言，在乾燥模式下，循環氣流冷 卻至露點以上，如此該循環氣中只有氣相存在。在冷凝模 式下，循環氣被冷凝至露點以下，在特定條件下形成一種 兩相的氣液混合物，如此，至少在流化床反應器的入口處 一直到液相揮發或是進入流化床之間，該混合物中的液相 夾帶於混合物中的氣相中。 循環氣進入流化床的位置一定位於流化床（聚合區） 的下方’以保證上游氣流的均勻性以及床層的懸浮狀態。 循環氣進入流化床的位置一般位於反應器較低的位置，最 好是反應器的底部，以保證經由流化床的上游流體的均勻 性。 在循環氣入口附近安置一種隔板或是類似的設備用於 -25 - 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） 523647 A7 B7 五、發明説明（2¾ 防止產生低氣速區，使得固體和氣體物質繼續留在上游循 環氣流中。 (請先閲讀背面之注意事項再填寫本頁) 循環氣流可以被分隔爲兩股和多股氣流，其中一股或 多股氣流被直接引入聚合區，使其在流化床下和經由流化 床時具有足夠的氣速保持流化床的懸浮狀態。在所有情形 下’循環熱都必須保持其成分的嚴格一致均勻，並且其流 動形式必須使得反應器內不存在生成不可移出固體物質之 死角。 將補償聚合單體以液體和/或固體的形式注入反應器 中能得到較佳之效果。本發明對在循環氣入口處或是反應 器的其他地方或是循環氣流中注入氣相或液相的補償聚合 單體的方法做出探討。 第2圖是本發明的非限制性實例。首先，必須指明的 是本發明的製程並不局限於某些具體的設備或是管線佈局 。例如，本發明的具體實例中示出的每個設備可爲多組的 多級或並列之設備。 經濟部智慧財產局員工消費合作社印製 第2圖示出的是根據本發明設計的流化床反應器，尤 其適用於生產聚烯烴樹脂的反應器。第2圖中，T I =溫 度指示器，TC=溫度控制器，〇p=輸出，SP=選定 値’ SC=速度控制器，pv=製程變數。反應器10包 括一個反應區1 2和一個減速區1 4。 一般而言，反應區的高度和直徑比一般較佳的變化範 圍是在2 · 7 : 1到5 : 1。當然，該範圍可以根據所需 的生產能力變大或變小。一般而言，減速區1 4的橫截面 本紙張尺度適用中國國家標準（CNS ) A4規格（210X 297公釐） _ 26 _ 523647 A7 B7 五、發明説明（d 積比反應區1 2的橫截面積約大2 . 6到2 . 8倍。 反應區1 2包括一個聚合物顆粒生長床，形成的聚合 物顆粒及少量的觸媒顆粒在經由反應區的以補償原料的形 式存在的可聚合的和調整後的氣態成分的連續氣流和循環 氣的作用下流化於床層上。爲了維持合適的流化床，經由 床層的表面氣速必須高於流化要求的最低流速，較佳的表 面氣速至少必須高於流化要求最低流速約〇 · 2 f t / s 。一般而言’表面氣速不高於5 · 〇 f t/s，通常 2 . 5 f t / s就足夠了。 重要的是，流化床中總含有某些顆粒，用於防止局部 “熱點”的形成，並且用於在整個反應區內引入並且分散 某種特定的觸媒。一開始，在通入氣流之前，反應器種通 常加入某種特定的聚合基質材料。這些顆粒可以與要合成 的聚合物相同或不同。當其與合成產物不同時，彼等與合 成的聚合物一起作爲初產品一起流出反應器。最後，所需 合成聚合物顆粒的流化床代替了一開始的流化床。 流化床中的部分的或完全活化的原料和/或觸媒最好 儲存在記憶體1 6中備用，例如一個或多個由速度控制器 S C控制的觸媒進料器1 6在對儲存材料呈惰性的保護氣 氛下’如氮氣或氬氣。如以下將進一步具體描述的，記憶 體最好包括兩個觸媒進料器。 流化狀態是經由高速的流體循環並且經由床層來實現 的，一般是補償原料流流速的2 0到7 0倍，通常是3 0 到6 0倍’最常見的是4 0倍。流化床一般形貌是浸沒於 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） (請先聞讀背面之注意事項再填寫本頁) -一切 丁 經濟部智慧財產局員工消費合作社印製 523647 A7 _____ B7 五、發明説明（2έ (請先閱讀背面之注意事項再填寫本頁) 經由反應器的氣流的單獨移動的密相顆粒。床層的壓降等 於或是略大於被橫截面分隔的流化床重量。如此，壓降取 決於反應器的幾何形狀。 補償流體在位置1 8注入流化床。補償流體的成分是 由一個氣體分析器決定的。氣體分析器2 1測定循環氣的 成分，根據測定値調整補償流體的成分，用以維持反應區 內穩定的氣相組成。氣體分析器有大量的市售來源。一般 而言，氣體分析器放置於能夠分析減速區1 4和熱傳輸區 2 4之間氣體的位置。 爲了保證完全流化，循環流和，如果需要，部分的補 償氣流經由循環管2 2在床層下的2 6位置回流入反應器 中。在回流位置的上方加上一個分散板輔助床層流化能夠 得到較佳的效果。循環氣經由流化床時，吸收由聚合反應 生成的反應熱。 組成循環氣的在流化床上不發生反應的那部分流態物 質離開聚合區後，最好經由一個減速區，使得其中的固體 顆粒可以有機會落回到流化床上。 經濟部智慧財產局員工消費合作社印製 然後循環氣在壓縮機3 0中壓縮，且然後經由一個熱 傳輸區，在循環氣回到流化床前交換其中的反應熱。熱傳 輸區一般是一個熱交換器2 4，例如水平型或是垂直型。 然後，循環氣流在反應器的底部2 6回到反應器中’經由 氣體分配板2 8進入流化床。一種氣體變流裝置通常安裝 在反應器的入口處，防止其中的聚合物顆粒流出或是聚集 成團。 -28- 本紙張尺度適用中國國家標準（CNS ) Α4規格（210Χ297公釐） 523647 A7 B7 五、發明説明（2έ (請先閲讀背面之注意事項再填寫本頁) 在穩定的狀態條件下，經由經常的移除反應熱，將流 化床的溫度控制在一個固定値。在流化床的上部沒有明顯 的溫度梯度。溫度梯度一般存在於流化床底部的入口流體 溫度與床層上殘留物之間的區間上，一般是4 8英尺高（ 1.2米），尤其是24英尺（6 lcm)，更常見的是 位於12英尺高（3 0 cm)。溫度梯度典型者爲高達約 5 0 °C，更典型者高達約3 0 °C，典型範圍爲約1 〇 -2 0 °C。 良好的氣體分散在反應器操作過程中具有重要的作用 。流化床包含正在生長的和已經形成的聚合物顆粒，和觸 媒顆粒。因爲，聚合物顆粒是熱的，而且可能還有活性， 彼等必須避免被靜置，因爲一旦存在靜止的塊狀物質，其 中的活化的觸媒將進一步反應，導致其融化。因此，將循 環氣流以足夠高的速度經由流化床以保持其流化狀態是很 重要的。 經濟部智慧財產局員工消費合作社印製 氣體分配板2 8是獲得良好氣體分配效果的一種設備 ，其可爲一種篩網、槽形板、多孔板、泡罩形板等等。該 板的所有元件可爲固定的，或是如Di DRU SCO的美國專利 第3，298，792號所述之活動型的板，其揭示內容 以引用方式倂於本文。 無論如何設計，氣體分配板是用來分散循環氣，令其 經由流化床底顆粒，使流化床保持流化狀態，同時可以在 反應器不運轉時，維持一個穩定的樹脂顆粒床。 任何一種對觸媒和反應物呈惰性的流體都可以用於循 本紙張尺度適用中國國家標準（CNS ) A4規格（210 X 297公釐） _ 29 _ 523647 A7 B7 五、發明説明（ 環氣中。具體實例包括飽和烴，例如烷烴，例如異戊院， 正戊烷，異己烷，正己烷。 (請先閲讀背面之注意事項再填寫本頁) 如果使用一種或多種觸媒，例如一種或多種共觸媒， 從熱交換器2 4下行加入反應系統中能夠獲得較佳的效果 。如此’觸媒可以經由管道4 0經分散器注入反應系統中 。典型的共觸媒是院基錦，如三乙基銘（teal )、三 甲基鋁（tma)、三丁基鋁、甲基鋁氧烷（ma〇）等 等。如此的觸媒可以用於齊革勒-納塔反應和金屬茂催化 系統。 流化床反應器最好在聚合物顆粒的燒結溫度以下工作 ，以確保燒結不會發生。燒結溫度是樹脂材料密度的函數 。例如，一般而言，低密度樹脂聚乙烯燒結溫度較低，而 高密度聚乙烯樹脂具有較高的燒結溫度。例如溫度範圍在 7 5 °C - 9 5 °C適用於生產密度範圍在約〇 . 9 1 一 0.95g/cm3的乙烯共聚物，而溫度範圍1〇〇一 115°C適用於生產密度範圍〇 . 95 — 0 . 97g/ c m3的乙儲共聚物。 經濟部智慧財產局員工消費合作社印製 流化床反應器可以在超過1 0 0 0 p s i ( 6 · 9 M p a )的壓力下工作。對於聚烯烴產品，反應器 的工作壓力在約100 — 400psi (0.69到 2 . 8 M p a )，更好的工作壓力在200- 4 0 0 p s i ( 1 · 4 — 2 · 8 M p a )，最好的是在約 250-350psi ( 1 . 7 - 2 . 4 M p a )，在如 此的高壓條件下有利於熱傳輸，因爲壓力提高可以提高單 -30- 本紙張尺度適用中國國家標準（CNS ) A4規格（210'乂297公釐） 523647 A7 B7 五、發明説明（2¾ 位體積氣體的熱容。正如在發明背景中提到的，當需要提 高循環氣的露點時可以加大工作壓力。 (請先閲讀背面之注意事項再填寫本頁) 經濟部智慧財產局員工消費合作社印製 部分活化的或完全活化的原料和/或觸媒（此後，全 部簡要的稱之爲觸媒）注入導管4 2或者可以在分散器 2 8上的4 4位置以其消耗的速率注入反應床中。較佳的 是，觸媒注入反應器中的位置能夠與良好混合之聚合物遭 遇。在分散器上方位置加入觸媒能夠較好的滿足流化床聚 合反應器的工作要求。因爲，觸媒是高度活化的，在分散 器下方位置注入觸媒將使聚合反應發生在那兒，並且最終 導致分散器的堵塞。另外，在分散器的上方位置注入觸媒 可以有助於觸媒在反應床上分散，避免由於高觸媒濃度產 生局部濃度過高，形成“熱點”。在反應床的上方注入觸 媒會導致過多的觸媒進入循環管道，在其中發生聚合反應 ，堵塞管道，最後導致熱交換器的堵塞。因此，觸媒注入 反應器的位置一般位於距離反應器壁反應器直徑的1 0 -5 0%，較好的是1 5 — 40%，最好是20 — 3 5%， 其高度約爲反應床高度的5 - 3 0%，較好的是5 - 2 5 %，且最好是5 — 15%。 觸媒可以採用多種技術注入反應器。但是，其中效果 較佳的是CALVERT等人的美國專利第3，779，712 號中的觸媒連續注入反應器之方法，其揭示內容以引用方 式倂於本文。 第3圖是根據本發明之方法可使用之觸媒進料器1 6 。觸媒進料器1 6類似CALVERT等人專利中所述之觸媒進 -31 - 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） 523647 A7 B7 五、發明説明（2¾ 料器。不同的是，觸媒進料器1 6中包含兩個霧沬室或區 塊4 6。 (請先閲讀背面之注意事項再填寫本頁) 第4圖是觸媒進料器1 6的裂開的部分橫截面圖。觸 媒在觸媒進料器1 6的較低的容器4 8中。該較低的容器 .4 8中包含兩個眼p 〇 r t 5 0。在較低容器的下方是一 個帶有腔5 4的流量盤5 2。流量盤5 2可以在轉動柄 5 6的帶動下轉動。流量盤的下方是一個帶有兩個入口的 較低位置的輪5 8。每個入口都分別和一個區塊4 6相連 0 觸媒進料器1 6的功能基本與CALVERT等人所述之觸 媒進料器相似。一般而言，當流量盤轉動時，經由管5 0 每個腔5 4中都會盛滿觸媒。然後，當盛滿觸媒的腔5 4 和入口 6 0呈一條直線時，觸媒就被引入區塊4 6中。如 此，觸媒'進料的速度就可以經由轉動流量盤5 2來控制。 較佳者爲使用一種對於觸媒呈惰性的氣體，如氮氣或 氬氣，將觸媒帶入反應床中。 經濟部智慧財產局員工消費合作社印製 該床中的聚合物生產速度取決於觸媒的注入速度以及 循環氣中單體之濃度。但是，一些約束變數能夠影響達到 的最大反應速率的値。具體的約束變數包括，但不限於： 冷卻水△溫度（有效吸熱値）、循環氣露點、用於使反應 床保持良好流化的可允許的最大惰性冷卻劑的値、冷卻劑 離開反應器之速率。本發明對於上述的每個約束變數都是 同樣有效的。如此，本發明係關於根據一個或多個上述變 數對反應速率進行控制。具體的這些約束變數的實例包括 -32- 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） 523647 Α7 Β7 五、發明説明（3ί) (請先閱讀背面之注意事項再填寫本頁) 合意生產速率、有效熱傳輸，其隨著外界條件改變而改變 (如，冷卻水△ Τ，冷卻水閥位置，經由冷卻塔之流速） 、露點邊界、冷凝物重量百分比、可冷凝物重量百分比、 產品移出（如吹掃箱水位）、流化程度、夾帶程度、造粒 器、粒狀樹脂輸送能力和進料（如進料壓力）。 在氣相聚合反應中，其中一個經常達到的約束變數就 是有效冷卻。有效冷卻測定的一個重要的手段就是進入熱 交換器冷卻水溫度與冷卻水的初始溫度之間的溫差。冷卻 水進入熱交換器的溫度指的是“混合點”，即在補償冷卻 水與循環水在循環管道內混合。爲了測定有效冷卻，採用 以下的冷卻水△ T ( C W D Τ )的定義： C W D Τ = “混合點”水溫一供水溫度 經濟部智慧財產局員工消費合作社印製 當C W D Τ接近零時，就到達了冷卻的理論上限，例 如，當冷卻水閥7 0全開並且在第2圖所示的冷卻系統中 超過9 5 %的經由冷卻塔的水。由C W D Τ測定的有效冷 卻和觸媒進料改變之間的動態關係是本發明的生產速率控 制器設計的一個很重要的方面。 第5圖是一個表示氣相聚合反應生產速率控制器邏輯 的非限制性實例的總圖，其中生產的約束變數包括目標生 產速率、冷卻水△ Τ、冷卻水閥7 0位置和露點。但是， 本發明中的控制系統的構造還可以擴展到能實現本發明目 的之方法。 -33- 本紙張尺度適用中國國家標準（CNS ) Α4規格（210Χ297公釐） 523647 A7 ___ B7___ 五、發明説明（3) (請先閲讀背面之注意事項再填寫本頁) 在第5圖中，速率控制器中較佳的是包括一種計算程 式。因此，本發明較佳的是包括一種數位電腦用以根據測 定的製程參數和輸入到電腦的預設値計算需要的控制信號 。本發明可以作爲一種分散控制系統（D C S )( distrbuted control system)的一部分。根據本發明，市售 的該系統的實例包括Foxboro IA (智慧自動控制）和 Honerwell TDC-3000。其他型號的控制系統也可以用在本 發明中。 速率控制器1 0 0是根據目標生產速率1 0 2、目標 冷卻水閥位置（CW Valve Position) 1 〇 4和一個目標露 點（DewPt) 1 〇 6來編程的。如此，操作者詳細輸入生產 速率、冷卻水閥7 〇位置和露點這些約束變數的接近極限 的目標數値。根據歷史資料，速率控制器1 0 0自動的將 冷卻水閥位置1 0 4翻譯爲合適的冷卻水△ T接近極限。 速率控制器1 0 0將測定的生產速率1 1 0和目標値 進行比較，測定的冷卻水閥位置（CW Valve Position) 經濟部智慧財產局員工消費合作社印製 1 1 2與測定的冷卻水△ T ( C W D T ) 1 1 4比較，測 定的露點（DewPt) 1 1 6與目標値進行比較。冷卻水閥位 置7 0與C W D T的比較中包括以下具體討論的級聯邏輯 ，參照第7圖。 速率控制器經由信號1 2 2與操作者介面相互作用。 操作者介面包括，例如，一個監視器和一個鍵盤。操作者 經由操作介面1 2 0輸入需要的預設値。 速率控制器還經由信號1 2 8和觸媒進料平衡控制系 -34- 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） 523647 A7 _______B7 ___ 五、發明説明（d (請先閲讀背面之注意事項再填寫本頁) 統相互作用。根據設備的動態回應信號，觸媒進料器平衡 控制器1 3 0的控制邏輯計算得到總的觸媒R PM優化目 標値’然後平衡分到正在運行的觸媒進料器的b丨〇 c k中。例 如’ C W D T和觸媒進料速率之間關係的歷史資料經分析 得出其中得動態回應。市售的動態分析軟體如〇H Cincinnai的 Arton公司的“PIT0PSTM，，能用於計算所有的約 束變數的動態轉移函數。分析顯示，冷卻水△ T的動態變 化的資訊足夠用於確定控制器的製程動態。 觸媒進料平衡控制器1 3 0經由信號1 3 2同一個區 塊和一個進料器啓動初始化控制邏輯1 4 0之間相互作用 。區塊和進料器啓動初始化控制邏輯1 4 0用於使手動操 作與自動控制之間變化平穩。 經濟部智慧財產局員工消費合作社印製 區塊和進料器啓動初始化控制邏輯1 4 〇將一個 RPM信號1 42傳輸給RPM P I D (比例一積分— 微分(proportional-integral-derivative))控制器工 5 0 。該R Ρ Μ Ρ I D控制器1 5 0將現時進料器R ρ μ 1 5 2與從區塊和進料器啓動初始化控制邏輯1 4 〇得到 的R Ρ Μ信號比較，並且計算出一個r ρ Μ信號1 5 4， 傳輸給控制該觸媒進料器的馬達控制觸媒進料速率。 使用第5圖示的控制邏輯，如果需要最大化生產速率 ’操作者必須給出一個目標生產速率1 〇 4的高預設値。 控制器1 0 0就會提高觸媒進料器RPM直至達到其他的 預設値的邊界，然後維持該R Ρ Μ値。換句話說，如果生 產速率最大化’那麽需要具體給出一個高的無法達到 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） ~ -- 523647 A7 _______ B7_ 五、發明説明（3$ (請先閲讀背面之注意事項再填寫本頁) 的預設値。如此，觸媒進料器就會加速以達到設定生產速 率値。當生產速率上升，接近其他約束變數邊界。約束 p I D値就會低於生產速率P I D ;降低觸媒進入反應器 的進料速率。例如，受限的約束變數通常是有效冷卻。有 效冷卻採用冷卻水法門7 0位置和C W D T連續的監測其 動態。 第5圖還示出了冷卻潛能損失警報器1 6 0。無論何 種原因，如果C W D T快速上升，·高優先順序警報器 1 6 0對操作者發出警告。CWDT的突然上升可能是因 爲原料中未知的有毒物質，不良觸媒或是其他的導致反應 衰減的原因。在這種情況下，不希望提高觸媒進入反應器 的流速。警報能對操作者反應即使的問題，提醒檢查反應 器條件，採取合適的措施包括取消自動控制。 第5圖進一步展示了一種CWD T偏離高優先順序警 報器1 7 0。該高優先順序警報器對操作者發出了潛在失 控警告。如果反應突然失控，表現在CWDT減小速率迅 速上升，或冷卻水閥快速打開，都能引發警報。 經濟部智慧財產局員工消費合作社印製 第6圖，反應器冷卻系統可以包括一個第一冷卻水泵 8 0和一個第二冷卻水泵8 2。第5圖還示出了 CW泵邏 輯控制（自動啓動備用泵）1 80。 在第一冷卻水泵工作失敗的情況下，控制邏輯自動推 薦啓動二級（備用）泵8 2。基於多個輸入的運轉泵8 0 的△壓力、馬達的開/關等級、泵的流出壓和其他可能輸 入値，自動觸發邏輯。如果其中的任意一個輸入値表示栗 -36- 本紙張尺度適用中國國家標準（CNS ) A4規格（21〇、〆297公釐） 523647 A7 B7 五、發明説明（ 工作失敗，備用泵8 2就會自動啓動。如此，備用泵8 2 在反應器運轉的條件下，運轉的泵8 0發生以下任意情況 時將啓動：泵8 0的低△壓力、低的馬達k W或a m p s 、開轉變爲關、反饋信號顯示馬達“未運轉”、由分散控 制系統警報探測到的中斷請求。另外，第二泵8 2在正常 情況下可以低速運轉，在第一泵工作失敗的條件下提高器 運轉速度。當兩個泵都無法正常運轉的條件下，邏輯控制 將自動關閉反應器。 第7圖是一個另一個表示氣相聚合反應生產速率控制 器邏輯的非限制性實例的總圖，其中生產約束變數包括所 需之生產速率、所需吹掃箱水位、冷凝物重量百分比最大 値、冷卻水閥7 0最大位置。在這點上，吹掃箱是產品進 一步處理前的暫時的存放地。 第7圖中，一個低信號選擇器2 0 0選擇多個約束變 數中的最低値作爲限制生產的約束變數。低信號選擇器 2 0 0和位於低信號選擇器2 0 0上方的P I D控制器一 起，實現第5圖中速率控制器的作用，以下將進一步描述 〇 第7圖的選定信號包括一個需要的生產速率2 0 2、 一個需要的吹掃箱水位2 0 4、冷凝物重量百分比最大値 2 0 6和一個允許的冷卻水（CW)閥最大位置2 0 8。 所需生產速率2 0 2和測定的現時的生產速率2 1 0 在一個P I D生產速率控制器（PRAT C) 2 1 2中進 行比較，該控制器將生產速率信號2 1 4送入底薪好選擇 ---------41^— (請先閱讀背面之注意事項再填寫本頁) 訂 經濟部智慧財產局員工消費合作社印製 本紙張尺度適用中國國家標準（CNS ) A4規格{ 210X297公釐） -37- 523647 Α7 Β7 五、發明説明（β (請先閱讀背面之注意事項再填寫本頁) 器200中。生產速率控制器（PRATC) 2 12是反 向動作的（如果生產速率（Ρ V )上升，輸出値必須減小 )。輸出信號2 1 4是送入反應器的總的R Ρ Μ的量，經 由生產速率表示。 所需吹掃箱水位2 0 4和測定的吹掃箱水位2 2 0在 一個PID吹掃箱水位控制器（PBNLC) 222中進 行比較，該控制器將一個吹掃箱水位信號送入低信號選擇 器200中。吹掃箱水位控制器（PBNLC) 222是 反向作用的（如果等級（Ρ V )上升，輸出必須減小）。 輸出信號2 2 4是送入反應器的總的R Ρ Μ的量，經由吹 掃箱水位表示。 經濟部智慧財產局員工消費合作社印製 冷凝物重量百分比最大値2 0 6和測定的冷凝物重量 百分比2 3 0在一個Ρ I D冷凝物重量百分比控制器（ WCONC) 2 3 2中進行比較，該控制器相低信號選擇器 2 0 0送出冷凝物重量百分比信號2 3 4。冷凝物重量百 分比控制器（WCΟNC ) 2 3 2是反向作用的（如果測定的 冷凝物重量百分比230上升，輸出降低）。輸出信號 2 3 4是進入反應器的總的R Ρ Μ値’經由冷凝物重量百 分比表示。 在這點上，操作者設定最大冷凝物重量百分比作爲控 制器的預設値。當生產速率提高或其他製程條件變化，如 果接近上述預設値，邏輯控制自動調整觸媒RPM以維持 冷凝物邊界條件或使其低於預設値。雖然不希望限於經驗 ，多數時間，通常選擇一個其他的約束變數。 本紙張尺度適用中國國家標準（CNS ) Α4規格（21〇X297公鐘） -38- 523647 A7 — —_ B7 五、發明説明（3¾ 允許的最大冷卻水閥位置2 0 8和一個測定的冷卻水 閥位置2 4 0，其値可爲冷卻水閥7 0位置的平均値，在 P I D閥位置控制器（VALVC ) 2 4 2中進行比較，控制 器將閥位置信號2 4 4送到一個P I D冷卻水△ T控制器 (CWDTC ) 2 4 6中，該〇界0丁（：控制器同時接收一個 測定的冷卻水△ T信號2 4 8。閥位置控制器（VALVC ) 作爲一個主P I D並且是直接作用的（如果測定的C W閥 位置（P V )提高，輸出也必須提高）。冷卻水△ T控制 器（CWDTC ) 2 4 6作爲一個伺服P I D並且是直接作用 的（如果測定的C W D T提高，輸出加大）。閥位置信號 2 4 4是進入反應器的總的R P Μ，經由冷卻水閥位置表 示。Ρ I D冷卻水△ Τ控制器（CWDTC ) 2 4 6將有效冷 卻信號2 5 0，基於C W D Τ的總的R Μ Ρ送料値，送入 低信號選擇器中。 如此，由VALVC和CWDTC形成的串級控制環路是用於 測定和控制冷卻約束變數。放熱反應系統中冷卻約束變數 釋一個很重要的約束變數，一般是最重要的一個約束變數 。所有能夠改善約束變數操縱控制的設計都能夠直接的有 利於生產速率的最大化。 串級控制系統將由冷卻水閥7 0參數的非線性關係線 性化。基於觀察和經驗，可以確定超過C W閥7 0位置的 邊界値，超過該邊界値有效冷卻基本小到可以忽略。該位 置可以由CW閥位置6 5%開度變化至約8〇%開度’需 要由每個反應器和每個閥依靠經驗判斷。當C W閥7 0接 本紙張尺度適用中國國家標準（CNS ) A4規格（210 X 297公釐） _ 39 - I —------衣-- (請先閲讀背面之注意事項再填寫本頁) 訂 經濟部智慧財產局員工消費合作社印製 523647 A7 B7 五、發明説明（3} (請先閲讀背面之注意事項再填寫本頁) 近其最大限度，主-伺服P I D聯合控制器一起工作，有 效的減小觸媒進料速率。採用孤立的C W D T信號或是冷 卻約束變數的其他可變參數’如經由冷卻塔的流速，無法 有效的完成相同的工作。 經濟部智慧財產局員工消費合作社印製 通常，在CW閥7 0位置和CWD T之間有一種一對 一的關係。當反應器無法被冷卻時（C W閥7 0處於幾乎 全開的位置），C W D T處於最小値（飽和蒸汽與冷卻劑 的最小溫差點對應的是沒有額外冷卻）。包含VALVC和 CWDTC多級點的多級控制系統利用了這種關係。CWDTC是 一種線性信號，並且在相對的快調伺服（內部）環路中工 作較佳。當有效冷卻下降時，CWDTC伺服有效的減小其輸 出値，如此準確的作出合適的動作。雖然，CWDTC能在短 期範圍內作出正確的動作，但就長遠看來其沒有真正確定 冷卻邊界的能力。冷卻邊界可以經由平均C W閥7 0位置 更準確的判定。這是因爲閥位置無疑能夠準確的表示冷卻 能力（或lack of )。在VALVC控制器中採用閥位置的過濾 値並且採用其重置C W D T控制器的預設値聯合兩個控制 器的信號。聯合的多級控制器知道準確的冷卻邊界，並且 以合適的速度進行回應。VALVC控制器不能夠離開CWDTC 控制器單獨使用，因爲閥位置信號非線形程度很高’尤其 當閥位置開度大於7 5 %時（從最大化速率的角度看最令 人感興趣的區域）。經由在多級結構中採用這兩個控制器 ，能夠達到短期的和長期的目標， 因此，每個 PID 如 212，222，232， -40- 本紙張尺度適用中國國家標準（CNS ) A4規格（210 X 297公釐） 523647 Α7 Β7 五、發明説明（d (請先閲讀背面之注意事項再填寫本頁) 2 4 6的輸出値都是以觸媒進料速率爲單位的。因此，最 低信號選擇器2 0 0選擇四個P I D的最低輸出値（約束 變數輸出）。 最低信號選擇器2 0 0和一個設計的計算邏輯控制器 2 6 0經由信號2 6 2，其中包括四個P I D中的最低信 號’相互作用。該設計的計算邏輯控制器完成觸媒進料平 衡控制器1 3 0模組和第5圖的進料器的啓動和初始化控 制邏輯1 4 0的工作。 對於設計的計算邏輯控制器2 6 0，分別帶有獨立區 塊的兩個觸媒進料器1 6對控制的配置和啓動帶來了一定 的困難。特定的控制邏輯要求要有正確的啓動，局部到遠 端的（AUTO-PC AS (如多級程式））順利轉換。爲了保持 淸晰和易於維護，整個控制邏輯分爲四個主邏輯模組，如 ，R P Μ啓動邏輯，R P Μ分流（splitter )邏輯，預設値 處理邏輯和R P Μ 防終止邏輯。控制器可以根據平臺類 型，經由不同的方式實現。例如，該處所示的邏輯模組可 以在不偏離本發明範疇的條件下合倂或分開。 經濟部智慧財產局員工消費合作社印製 如第7圖所示，設計的計算邏輯控制器2 6 0受到一 個進料器1 開/關信號2 6 4，一個進料器2 開/關 信號2 6 6，一個區塊1 1開/關信號2 6 8，一個區塊 1 2開/關信號2 7 0，一個區塊2 1開/關信號2 7 2 ，和一個區塊22開/關信號274。進料器1 開/關 信號2 6 4和進料器2 開/關信號2 6 6分別表示進料 器1和2的開關狀態。區塊1 1開/關信號2 6 8和區塊 -41 - 本紙張尺度適用中國國家標準（CNS ) Α4規格（210Χ297公釐） 523647 A7 ___B7 五、發明説明（3¾ (請先閱讀背面之注意事項再填寫本頁) 1 2開/關信號2 7 0分別表示如第3圖中的第一觸媒進 料器的區塊4 6中的兩個區塊的狀態是運作的或堵塞的。 類似的，區塊2 1開/關信號2 7 2和區塊2 2開/關信 號2 7 4分別表示第3圖中的第二觸媒進料器的區塊4 6 的兩個區塊的狀態是運轉的還是堵塞的。 如參照第8圖更詳細揭示者，邏輯控制器2 6 0的 R P Μ啓動邏輯使控制器在操作者手動控制和自動控制之 間實現平穩轉換。同樣也可以參考本發明的附錄，其中包 括本發明的控制邏輯實例的術語列表。 第8圖中所示的使R Ρ Μ啓動邏輯控制器之非限制性 實例。該邏輯塊一般運行的掃描時間在1 - 6 0秒之間， 較佳的是5 - 3 0秒，最佳的是1 5秒。 經濟部智慧財產局員工消費合作社印製 一般而言，邏輯塊檢查觸媒進料器# 1和# 2是否準 備接收來自擴展控制操作的遠端預設値。當一個邏輯塊是 開的，進料器馬達正在運行並且相應的R Ρ Μ Ρ I D處 於自動和遠端的狀態並且未被啓動時，觸媒進料器能夠接 收遠端預設値。如果以上條件滿足，那麽二進位輸出標記 (6〇〇1和8〇〇2)設爲是與非（〇或1)。 然後，控制邏輯確定進入反應器的區塊總數。當一個 區塊進行反應器進料時，其狀態必須爲“開”，並且其相 應的進料器馬達正在“運行”。如此就可以計算總的進行 反應器進料的區塊數。 由所有“開”的區塊和“運行”的進料器得到的總的 R Ρ Μ値計算後寫入R〇〇 2。如果控制方案因爲沒有一 -42- 本紙張尺度適用中國國家標準（CNS ) Α4規格（210X297公釐） 523647 A7 _______B7 五、發明説明（扁 個區塊處於合適的模式而未在“預備，，狀態（無法切換爲 開）’那麽R〇0 2値（總的R ρ μ )寫入R〇〇 1。 (請先閲讀背面之注意事項再填寫本頁) R〇0 1用於初始化上游流Ρ I D輸出値。如果，控制方 案處於“預備”狀態，那麼r 〇 〇 2値就不會複製給 R 〇 0 1。 仔細參照第8圖，控制邏輯在gg]3 0 0處開始。在 3 0 2處，控制邏輯確定第一觸媒進料器的區塊1 1或 經濟部智慧財產局員工消費合作社印製 1 2是否爲開。如果兩者皆關，則B〇〇 1値在3 04處 爲非。如果’至少一個區塊爲開，在3 〇 6處，控制邏輯 確定第一觸媒進料器的馬達是否打開。如果第一觸媒進料 器的馬達未開，那麽B 0 〇 1値在3 0 4處設爲非。如果 第一觸媒進料器的馬達在3 〇 6處是開的，在3 〇 8位置 控制邏輯確定第一觸媒進料器的r ρ Μ Ρ I D是否處於 自動和遠端狀態並且未啓動。如果第一觸媒進料器的 RPM ΡIϋ未滿足處於遠端和自動模式及未啓動這一 條件’ Β 0 〇 1値在3 〇 4處設爲非。如果第一觸媒進料 器的R Ρ Μ Ρ I D値符合條件，即處於遠端和自動模式 及未啓動這一條件，那麽3 1 〇位置boo 1値爲是。 在3 2 0 ’控制邏輯判斷第二觸媒進料器的區塊 2 1或2 2是否爲開。如果兩者皆關，則b〇 〇 1値在 3 2 2處爲非。如果，至少一個區塊爲開，在3 2 4處， 控制邏輯確定第二觸媒進料器的馬達是否打開。如果第二 觸媒進料器的馬達未開，那麽B〇〇 1値在3 2 2處設爲 非。如果第一觸媒進料器的馬達在3 2 4處是開的，在 -43- 本紙張尺度適财麵家標準（CNS ) A4規格（21GX297公酱） 523647 A7523647 A7 ______B7 _ 5. Description of the invention (1) Field of invention (Please read the notes on the back before filling out this page) The present invention relates to a system and method for controlling the reaction rate by controlling the catalyst feed rate. A preferred embodiment of the present invention relates to a method and system for controlling a continuous exothermic process, such as optimization of the production rate when a gas phase polymerization is performed in a fluidized bed reactor. BACKGROUND OF THE INVENTION Various methods have been used to control the reaction. Among them, controlling the feed rate of the catalyst is the more commonly used method. In many chemical reactions, such as the polymerization of hydrocarbon monomers, catalysts are used to promote chemical reactions. It is well known that most reactions are sensitive to the amount of catalyst used, so that the purpose of controlling the reaction can be achieved by controlling the catalyst feed rate to the reactor. For example, U.S. Patent No. 4,162,894 to TRIBBLE discloses a method and apparatus for controlling the catalyst feed rate. TRIBBLE monitors the reaction conditions in the reactor and generates signals to control the motor to deliver a certain amount of catalyst into the reactor. Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs, T R I B B L E reveals that the catalyst can control the catalyst input according to the coolant temperature difference (△ T) controller. U.S. Patent No. 4,669,473 to AGARWAL discloses a control system for an ethylene polymerization reactor. AGARWAL revealed that the amount of catalyst entering the feed tube is controlled by a function of the concentration of the feedstock in the feed tube or the flow of the feedstock in the feed tube. AGARWAL revealed that the control equipment can optimize its process by maximizing the reactor temperature, catalyst flow rate, coolant flow rate, reactor outlet temperature, and maximizing polymerization in the reactor. Since this paper scale, Chinese national standards ( CNS) A4 specification (210X297 mm) 77] 523647 A7 B7 V. Description of the invention (2) (Please read the precautions on the back before filling this page). AGARWAL further revealed that the catalyst feeding equipment is controlled according to the total feed flow of the reactor, the maximum temperature of the reactor and the required product quality. AGARWAL also revealed the addition of multi-point control catalysts. U.S. Patent No. 4,8,18,372, to MAUL EON et al. Discloses an apparatus for catalytic cracking of a hydrocarbon feedstock with reaction temperature control. MAULEON et al. Disclosed a valve controlled by a temperature sensor for regulating the injection rate of a regenerated catalyst. GROSS et al., U.S. Patent Nos. 4,093,537 and 4,21,6,36 describe a liquid catalytic control component. The GROSS et al patent discloses a method for adjusting the catalyst flow rate based on the reactor temperature. The GROSS et al. Patent also discloses a method for controlling the recycle ratio of the regeneration catalyst based on the temperature of the regenerator to compensate for the catalyst loss. Printed by the Consumers' Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs, GROSS et al., US Patent No. 4,282,084, discloses a catalytic cracking process. GROSS et al. Disclosed a calculation method for controlling the total amount of catalyst, for example, by controlling the regeneration of the catalyst, in this method controlling the required oxidation activity to obtain a suitable C02 / C0 ratio. GROSS et al. Revealed that feed and catalyst activity data were registered in the execution optimizer of the optimized process. GROSS et al. Revealed a temperature controller that collects data on reactants and reactor temperature to control the flow rate of the catalyst. U.S. Patent Nos. 5,883,292 and 5,9 39,5 8 2 of D AS SEL et al. Disclose methods for controlling the reaction by regulating condensation in the reactor. The patent of DASSEL et al. Reveals that the catalyst concentration is controlled based on various variables including the reaction temperature to control the conversion rate and the first dew point. -5- This paper size applies the Chinese National Standard (CNS) A4 specification (210X297 mm) 523647 A7 B7 V. Description of the invention (3) US Patent Nos. 6, 1 3, 6 9 8 by VASSILIOU et al. (Please read the precautions on the back before filling this page) to reveal a device that achieves control by adjusting the pressure drop rate Reaction rate of a hydrocarbon with an acid or other intermediate oxidation product. VASSILIOU et al. Adjusted the pressure drop rate to control the reaction rate by adjusting the feed rate of various components, including the catalyst, according to multiple variables, such as the composition of the circulating flow and the flow rate of the circulating flow. VASSILIOU et al. Monitored the reaction temperature and adjusted the heat exchanger to achieve the appropriate reaction temperature. U.S. Patent No. 4,619,901 to WEBB et al. Discloses a polymerization reaction based on a non-linear control signal obtained by comparing actual and desirable unreacted monomer concentrations to adjust the catalyst feed rate. The unreacted monomer concentration of the spill was maintained at the desired concentration. SCHMIDT et al. U.S. Patent No. 4,62,049 discloses a method for controlling the molecular weight of polybutene. SCHMIDT et al. Adjusted variables such as the feed rate of the catalyst into the reactor based on the isobutene concentration in the reactor. Printed by MAMEDOV et al., US Patent No. 5,116,915, etc., by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economics, discloses a method of computing the Mooney viscosity using a computer to adjust process parameters such as the feed rate of the catalyst. MAMEDOV et al. Also revealed that a computer is used to maintain the temperature difference between the reactor components to obtain the polymer with the desired molecular weight distribution. U.S. Patent No. 4,251,503 to SWINDELLS et al. Discloses an automatic and continuous monitoring system for the production of chlorine dioxide. SWINDELLS et al. Changed the catalyst feed rate based on the ratio of chlorine dioxide and chlorine in the exhaust gas. Other background references include European Patent 0906682 and US Patent Nos. 6,063,877 and -6-This paper size applies Chinese National Standard (CNS) A4 (210X297 mm) 523647 A7 B7 V. Description of Invention (4) 4 , 543, 399. ---------- 41 ^ 衣-(Please read the notes on the back before filling out this page) In a gas phase polymerization reactor, the reaction takes place in products such as granular polyethylene, and gaseous reactions Formation of fluid on a fluidized bed. The catalyst is injected into the fluidized bed. Reaction heat is transferred via a circulating gas stream. This air stream is compressed and cooled in an external circulation pipe. A compensating feed stream is passed in to maintain the required reactant concentration. Compared to stirred bed reactors and impeller reactors, in a fluidized bed reactor, the uniform distribution of reaction monomers and catalysts in the upstream gas stream is Hot spots and polymer fouling play a key role. See, for example, U.S. Patent No. 3,799,036. A further requirement for fluidized bed reactors is that the gas flow rate through the reactor must be able to maintain the flow state of the bed. The gas flow rate to maintain the fluidized suspension state of the fluidized bed cannot be achieved by merely relying on the injection of liquid at the bottom of the bed under normal conditions. Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs. Figure 1 is a schematic diagram of a well-known gas phase reactor system. The polymerization reaction is essentially a highly exothermic reaction. When the polymerization monomers are combined with each other to form a large complex molecular chain (polymer), the reaction heat is released. The reaction heat needs to be transmitted outward from the reaction site via convection, otherwise it will cause local temperature to be too high, generate hot spots, polymer agglomeration or melting. As such, temperature control is critical for stable reactor operation. Moreover, the main factor limiting the reaction rate in a fluidized bed reactor is the ability to remove reaction heat from the polymerization reaction zone. The polymerization reactor uses a gaseous medium to disperse the catalyst. The medium has two functions, both as a reaction carrier and as a cooling medium, removing the reaction heat from the activated position of the growing polymer. The general heat dissipation method used in a common fluidized bed reactor is to apply the Chinese National Standard (CNS) A4 specification (210 X 297 mm) to the paper size of the paper. 523647 A7 B7____ V. Description of the invention (5) External Compress and cool circulating airflow. Depending on the degree of cooling, the reactor system can be operated in a condensation mode or a dry mode. In the condensing mode, the two-phase fluid mixture is returned to the reactor by cooling the circulating gas below its dew point, thereby improving the heat dissipation capability of the circulating gas. In the dry operation mode, after the circulating gas is cooled above the dew point, a single-phase circulating gas, that is, the gas phase, is returned to the reactor. Referring to Figure 1, the operating mode of the system includes a return cooling water (C W R) valve in a servo loop operated by a cascade temperature controller of the reaction bed feed temperature to regulate the temperature of the water entering the heat exchanger. Variables in this temperature control process include a single loop bed temperature controller that directly operates the CWR valve. In addition, the operator can adjust the catalyst feed rate to maintain the largest possible reaction rate. In a large-scale fluidized-bed reactor for the production of polymers such as polyethylene, the amount of fluid that takes away the heat of polymerization via circulating cooling must be greater than the amount used to maintain the fluidized state of the fluidized bed and mixed into the fluidized bed. The amount of fluid required for solids. There is an upper limit to the flow rate of fluid in the reactor to prevent excess solids from being entrapped. When the heat of polymerization reaction (their heat ratio is directly proportional to the rate of polymerization reaction) is equal to the heat absorbed by the fluid flowing through the reactor plus the heat loss of other ways', a stable bed temperature can be obtained. A specific commercially available gas phase reactor system is the Unipo | TM system developed by Union Carbide. Heat transfer at the reaction site is accomplished via a heat exchanger using water as a cooling medium. The maximum production rate in the reactor is determined by the speed of heat transfer. The heating rate can be obtained by the following formula: Heating rate = QrPrate = MgCp (Tr-Tf) = MwCpw (Twi-Tw.) --------- Clothing-(Please read the precautions on the back before filling this page ) Order printed by the Intellectual Property Bureau of the Ministry of Economic Affairs, Consumer Cooperatives. The paper size is applicable to the Chinese National Standard (CNS) A4 specification (210X297 mm) -8-523647 A7 B7 V. Description of the invention (6) Fill out this page again) Among them is the reaction heat generation rate (when polyethylene is produced, it is about l525Btu / lb. (847kal / kg)); p "ate is the generation rate of the polymer; Mg is the mass flow rate of the reaction gas (reactants plus inert components); C p is the average mass heat capacity of the reaction medium; T r is the reaction temperature T f is the circulating gas feed temperature; μ w is the mass flow rate of the cooling water; T w ί is the water temperature at the heat exchanger inlet; τ w. Is the water temperature at the heat exchanger outlet. Pressure, feed level and composition adjustment control system. In general, in order to maximize the production rate of a reactor, the operator can manually adjust the catalyst feed rate (RPM) within the cooling limit range. Ministry of Economic Affairs wisdom It is a challenge that operators must face to maximize the production rate of the reactor within the limit of cooling by the Consumer Cooperative of the Property Bureau employee. Due to the change of day and night temperature and seasonal temperature, the entering temperature of cooling water changes periodically. Any possible feedup block down caused by the unstable operation of the catalyst feeder (c CF) and removing the feeder in order to re-add the catalyst propose another method to maximize the production rate. Challenge. Changes in the heat capacity of the reaction gas (eg via injection of isopentane) will also change the cooling water requirements in the heat exchanger. 0 Different catalysts are used in different polymerization processes, including Ziegler (Natta) catalysts, Chromium alloy and metallocene (metal) catalysts. The reaction catalysts can be single-phase or multi-phase, such as supported Ziegler (natta) or chromium alloy catalysts. Due to the difference in kinetic properties of each reaction Very far away, these catalysts are applicable to -9- this paper size applies Chinese National Standard (CNS) A4 specification (210X297 mm) 523647 A7 B7 V. Description of invention (7) (Please read the precautions on the back before filling this page) The response time for changing the feed level is different. Therefore, it is a complex optimization problem for the operator to maintain a maximum and safe reaction rate at all times. The operator must estimate in advance to increase the catalyst feed Rate, while ensuring that the reactor is properly cooled within the previously-constrained constraints. For operators, there has been a trend when additional cooling is needed They usually maintain the system in a "comfort zone," which refers to an area with excess cooling capacity. Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs, as described above, the fluidized bed reactor can be dried Run in condensing mode or condensing mode. In dry mode, the circulating airflow is cooled to above the dew point, so that only the gas phase exists in the circulating airflow. In condensing mode, the circulating airflow is cooled below the dewpoint, forming a gas-liquid coexistence under specific conditions The mixture is at least at the entrance of the fluidized bed reactor until its liquid phase is volatilized or enters the fluid phase of the mixture. The liquid phase in the mixture is mixed with the gas phase of the mixture. The condensation mode can produce space-time. The rate has increased significantly, while the properties and quality of the products obtained have not changed much or remain the same. The cooling temperature of the condensed mixture is controlled to a degree below the dew point by controlling the temperature of the outlet of the heat exchange zone of the circulating circulation to achieve the required degree of cooling. Obviously, if required, it is also possible to inject the gas and liquid separately into the reactor under specific conditions to form a two-phase fluid. By operating in condensing mode, the fluidized bed reactor can be cooled by cooling the circulating stream below the dew point, and the resulting two-phase fluid is returned to the reactor to maintain the fluidized bed reactor at a desired higher than the circulation Temperatures above the dew point of the fluid increase the space-time yield of the polymer. Cooling of circulating fluid-10- This paper size applies Chinese National Standard (CNS) A4 specification (210X297 mm) 523647 A7 B7 V. Description of the invention (8) The capacity depends on the temperature difference between the inlet of the circulating flow and the reactor and The degree of volatility of the condensed liquid in the circulating fluid. (Please read the precautions on the back before filling out this page.) From the above, we can know that the process of controlling reactions, such as fluidized bed reactions, is usually a manual operation. As a result, response control is often tedious, inaccurate, and subjective. Although reactive automatic control systems are available, there is still a need to improve them. Summary of the Invention In a specific example, the present invention relates to a system and method for optimizing the reaction rate of a polymerization reaction performed in a fluidized bed reactor. The invention also relates to a method and system for identifying important variables in a reaction automatic control process. Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs, the present invention is further related to controlling the catalyst feed rate by controlling the increase or change of process variables that may be caused during the operation of the reactor, so as to control the exothermic or endothermic reaction process. Methods and systems. As is well known to the artist, these variables are commonly referred to as process-constrained variables. It is generally desired that the chemical process in the reactor be performed safely and efficiently by adjusting and controlling these process constraints. For example, in an exothermic reactor, the variables that need to be adjusted and controlled include: reactor production speed, effective heat transfer (derived from the function of the ΔT of the coolant), the dew point of the reactor inlet and the weight percentage of condensed material . The purpose of the comprehensive constraint variable manipulation control scheme is to regulate and control the process constraint variables. There is only one major variable in the comprehensive constraint variable manipulation control scheme described here, and its precise control is the most important. Every comprehensive constraint variable manipulation control scheme must have one or more constraint variables, which are also specified by -11-This paper size is applicable to the Chinese National Standard (CNS) A4 specification (210 X 297 mm) 523647 A7 B7__ V. Description of the invention (9) (Please read the notes on the back before filling this page) It is called the second variable. In most and normal operating situations, the first control variable is a controlled variable. The second variable is generally outside its constraints, so no control is needed. In a specific example, such a means is generally referred to as single-constrained variable manipulation control. The constraint variable manipulation control uses the production rate as the first control variable in the control scheme. This specific embodiment provides a specific example of controlling the production rate to a fixed rate based on some considerations such as the supply-demand ratio. ΔT of cooling water, weight percentage of dew point or condensate, and purge tank water level are the second or constrained variables. In this specific embodiment, the main control variable is adjusted and controlled through continuous coordination, and the second variable is controlled and positioned simultaneously to make the control scheme more complete ''. In another specific example, constrained variable manipulation control provides a dual variable or dual system coupled with a constrained variable. This dual system monitors both the cooling water valve position and the cooling water ΔT upper limit. When catalyst changes, external conditions change, or an unpredictable disturbance affects the operation of the reactor (the latter usually occurs during typical gas phase polymerization), the dual system will help improve the stability of its control process. The improved control stability helps to increase the reaction rate. Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs In another specific example, the present invention relates to a reaction process constraint variable manipulation control method for optimizing a reaction rate, the method includes: according to effective heat transfer and at least one additional process constraint The variable automatically and continuously controls the feed rate of the catalyst into the reactor to achieve the purpose of controlling the reaction. This embodiment has its advantages because the exothermic reactor requires an external cooler for removing the heat generated by the reaction. Such reactor system installations have their cooling capacity limitations, and as is well known to the industry, these limitations have brought many paper sizes to the Chinese National Standard (CNS) A4 specification (210X297 mm) ~ Λ0-523647 A7 B7 V. Description of Invention (ΐά (Please read the notes on the back before filling this page). If the reaction temperature is too high, according to the design of the cooler, the cooler is at its maximum cooling limit. When it is at the cooling limit, the cooler The effective heat transfer rate is zero. This specific embodiment enables the reactor to be closer to the effective heat transfer zero according to its maximum production rate. In another aspect, the present invention is a reaction process constraint variable manipulation control system for optimizing the production rate The system includes a reactor, a catalyst feeder for adding a catalyst to the reactor, a heat transfer device for heat in the reactor, and an effective heat transfer sensing for determining effective heat transfer in the heat transfer device. The catalyst, at least one continuously and automatically controls the catalyst input according to the effective heat transfer amount and at least one additional process constraint variable. The controller of the feeder. In another aspect, the present invention relates to a method for manipulating control of a reaction process constrained variable that optimizes the production rate. The method includes: continuously and automatically controlling the catalyst feeder according to effective heat transfer; A warning is issued when the effective heat transfer exceeds a preset value after the change. The employee consumer cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs is printed in another aspect. The present invention relates to a response process constraint variable manipulation control system that optimizes the production rate. The system includes A reactor, a catalyst feeder for adding a catalyst to the reactor, a heat transfer device for exchanging heat in the reactor, an effective heat sensor for measuring effective heat transfer in the heat transfer device, at least A controller that continuously and automatically controls the catalyst feeder according to an effective heat transfer amount, wherein the controller issues a warning when the effective heat transfer changes beyond a preset threshold. In another aspect, the present invention relates to a method for A method for manipulating and controlling a constrained variable of a reaction process for optimizing a reaction rate, the method includes: Standard (CNS) A4 specification (210X297 mm) 523647 A7 B7 V. Description of the invention (1) The valve position of the transmission device continuously and automatically controls the rate at which the catalyst enters the reactor, thereby controlling the reaction. (Please read the precautions on the back before reading) (Fill in this page) In another aspect, the present invention relates to a reaction process constraint variable manipulation control system for optimizing the reaction rate. The system includes: a reactor, a catalyst feeder for adding a catalyst to the reactor, Heat transfer equipment for exchanging heat in the reactor, a heat transfer source, a conduit for transferring a heat transfer medium between a heat exchanger and a heat transfer source, and a bypass for at least part of the heat transfer medium The transmission source recirculates at least part of the heat transfer medium into the heat exchanger without passing through the heat transfer medium, a heat transfer medium valve for controlling the amount of bypass heat transfer medium and the amount of heat transfer medium via the heat transfer source A heat transfer medium valve sensor for determining the position of the heat transfer medium valve, an effective heat transfer for determining the effective heat transfer in a heat exchanger A sensor, at least one controller for controlling the catalyst feeder, wherein the heat transfer medium valve sensor is connected to at least one controller, and at least one controller for controlling the catalyst feeder The transmission medium valve position responds. The Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs is printed in another aspect. The present invention relates to a method for controlling and controlling the reaction process constraint variables for optimizing the reaction rate. The method includes: continuously and automatically controlling the catalyst to enter the reaction according to the following variables The feed rate of the reactor controls the reaction: effective heat transfer rate, the current production rate of the reactor, the amount of reaction products in the reactor collector, the mass percentage of condensate in the reactor circulating stream, where the reaction includes the formation of polyethylene with ethylene Of polymerization. In one aspect, the additional reaction constraint variables include the current production rate in the reactor. -14- This paper size applies the Chinese National Standard (CNS) A4 specification (210X297 mm) 523647 A7 _ B7_ _ V. Description of the invention (0 In another aspect, the current production rate is compared with the desired production rate to control contact Media feed rate. (Please read the notes on the back before filling this page.) In another aspect, the additional reaction constraint variable includes the amount of reaction products in the sampler in the reactor. In another aspect, the The amount of reaction product in the sampler is compared with the amount of reaction product in the required sampler to control the catalyst feed rate. In another aspect, the additional process constraint variables include the weight of the condensate in the circulating flow in the reactor. Concentration. In another aspect, the weight percent concentration of the condensate is compared to the weight percent concentration of the condensate of the desired recycle stream. In another aspect, the additional process constraint variables include the recycle stream in the reactor In another aspect, the dew point is compared to a desired dew point to control the catalyst feed rate. In another aspect, the additional process constraints variables Including the amount of solids entrained in the circulating stream. The Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs printed on the other side, comparing the amount of solids entrained in the circulating stream with the required amount of solid entrainment to control the catalyst feed rate In another aspect, the additional process constraint includes the granular resin delivery system rate. In another aspect, the granular resin delivery system rate is compared to the required granular resin delivery system rate. In order to control the catalyst feed rate, in another aspect, the additional process constraints include the pelletizing rate. -15- This paper size applies the Chinese National Standard (CNS) A4 specification (210 × 297 mm) 523647 A7 B7 V. Description of the invention (In another aspect, the granulation rate is compared with the required granulation rate to control the catalyst feed rate. (Please read the notes on the back before filling this page) In another aspect, the additional Process constraint variables include the feed stream. In another aspect, the feed stream is compared to the desired feed stream to control the catalyst feed rate. In another aspect, the basis is valid Heat transfer to automatically and continuously control the feed rate of the catalyst into the reactor includes monitoring the ΔT of the mixing point of the heat transfer medium. In another aspect, the automatic and continuous control of the feed rate of the catalyst to the reactor based on the effective heat transfer includes Monitoring the ΔT of the mixing point of the heat transfer medium and monitoring the position of the heat transfer medium valve of the heat transfer equipment. In another aspect, the automatic continuous continuous control of the feed rate of the catalyst into the reactor based on the effective heat transfer includes monitoring the heat transfer medium Valve position of the heat transfer medium of the reactor. In another aspect, the reactor includes a heat transfer device including a heat exchanger for heat transfer with the reactor, and a heat transfer medium in the heat exchanger A conduit that forms a loop with the heat transfer source. Printed in another aspect by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs, the heat transfer device includes a device for bypassing at least part of the heat transfer medium so that at least part The heat transfer medium is recycled into the recirculation duct of the heat exchanger without passing through the heat transfer medium source. In another aspect, the recirculation conduit is designed to mix at least a portion of the heat transfer medium with a heat transfer medium via a heat transfer source before entering the heat exchanger at a mixing point. -16- This paper size is in accordance with Chinese National Standard (CNS) A4 specification (210X297 mm) 523647 A7 _B7 _ V. Description of the invention (on the other hand, a first temperature sensor at the heat transfer source and mixing point The first temperature of the heat transfer medium was measured between two occasions; a second temperature sensor measured the position of the second heat transfer medium at the position between the mixing point and the heat exchanger (please read the precautions on the back before filling this page). Temperature 〇 In another aspect, a controller subtracts the first temperature from the second temperature to calculate ΔT. In another aspect, the controller issues a warning when ΔT changes above a predetermined threshold. In one aspect, the heat transfer device includes a heat transfer medium valve for controlling the number of bypass heat transfer sources and the amount of heat transfer medium via the heat transfer source. In another aspect, a heat transfer medium valve senses The device determines the position of the heat transfer medium valve. In another aspect, the position of the heat transfer medium valve is compared to the maximum heat transfer medium valve position that can be reached to control the catalyst feed rate, and the position of the heat transfer medium valve is The position of the heat exchanger can be affected when the position of the heat transfer medium valve is changed. Printed in another aspect by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs, the method further includes measuring the pressure caused by the first pump of the heat transfer equipment. In another aspect, the method further includes controlling the second pump based on the pressure differential generated by the first pump. In another aspect, the reactor includes a first-rate chemical bed. In another aspect, the The reaction includes a polymerization reaction. In another aspect, the reaction includes the polymerization of ethylene to form polyethylene. -17- This paper is sized to the Chinese National Standard (CNS) A4 specification (210 × 297 mm) 523647 A7 __B7_ V. Description of the invention (4 (Please read the notes on the back before filling out this page) In another aspect, the system also includes a heat transfer for controlling the number of bypass heat transfer sources and the amount of heat transfer media via the heat transfer source Medium valve, the system further comprises a heat transfer medium valve sensor for determining the position of the heat transfer medium valve, wherein the heat transfer medium sensor is connected to at least one controller At least one controller is used to compare the heat transfer medium valve position sensor and the AT model signal to control the catalyst feeder. In another aspect, the pressure difference sensor is connected to a second pump control Controller, the controller controls the second pump according to the pressure difference generated by the first pump, and the second pump controller is the same as or different from at least one controller. In another aspect, the system further includes a circulation circuit In another aspect, the system further includes a dew point sensor for determining the dew point of the gas in the circulation loop. In another aspect, the dew point sensor is connected to at least one controller, and wherein the At least one controller is configured to control the catalyst feeder based on the dew point of the gas in the circulation loop. The employee consumer cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs is printed in another aspect. The system further includes an operator interface for receiving a The dew point is close to 値, and at least one controller compares the dew point to 値 and the dew point to control the catalyst feeder. * In another aspect, the system further includes a condensate weight percent sensor for determining the weight percent of condensate in the circulation loop. In another aspect, the weight percentage sensor is associated with at least one controller. Connected, wherein the controller is configured to control the catalyst feeder based on the weight percentage of the condensate in the circulation loop. -18- This paper size applies to Chinese National Standard (CNS) A4 (210X297 mm) 523647 Α7 Β7 V. Description of the invention (ιέ (Please read the precautions on the back before filling this page) In another aspect, the system An operator interface is further included for receiving the maximum allowable condensate weight percentage, and the at least one controller controls the catalyst feeder by comparing the maximum allowable condensate weight percentage with the condensate weight percentage. In another aspect, the reactor includes a collector for collecting reaction products. In another aspect, the system further includes a reaction product sensor for determining the amount of reaction products in the collector. In one aspect, the reaction product sensor is connected to at least one controller, and the at least one controller is configured to control the catalyst feeder according to the amount of reaction products in the collector. In another aspect, the The system further includes an operator interface configured to receive the amount of reaction products in a collector required by the operator, wherein at least one controller is The catalyst feeder is controlled by comparing the amount of reaction product in the plutonium with the actual collector. In another aspect, the system further includes a production rate sensor for determining the production rate of the reactor. Ministry of Economic Affairs The Intellectual Property Bureau employee consumer cooperative is printed in another aspect, the production rate sensor is connected to at least one controller, and wherein the controller is configured to control the catalyst feeder according to the production rate. In one aspect, the system further includes an operator interface configured to receive the required production rate data, and at least one controller controls the catalyst feeder by comparing the actual production rate with the required production rate. -19- This paper size is in accordance with Chinese National Standard (CNS) A4 specifications (210 X297 mm) 523647 Α7 Β7 V. Description of the invention (A brief description of the drawings (please read the notes on the back before filling this page) The present invention will It is further elaborated below with reference to the attached numerous non-limiting diagrams, in which: FIG. 1 is a schematic diagram of a known gas phase reactor system; Fig. 2 is a schematic diagram of a gas phase reactor system obtained according to the present invention; Fig. 3 is a perspective view of a catalyst feeder; Fig. 4 is an exploded partial cross-sectional view of the catalyst feeder; Is a logic diagram where the production rate is controlled via the target production rate, cooling water ΔT, the cooling water valve position and the dew point; Figure 6 is a logic diagram that has been controlled by the target production rate, the target cooling water valve position and the target dew point Figure 7 is a logic diagram for controlling production via production rate hope, purge tank water level hope, maximum mass percentage of condensate and maximum valve position of cooling water; Figure 8 is a logic diagram of RP M initialization logic; Printed by the Intellectual Property Bureau of the Ministry of Economic Affairs, Consumer Cooperatives Figure 9 is a logic diagram of the RPM shunt logic; Figure 10 is a logic diagram of a given processor; Figure 11 is an RPM anti-blocking logic diagram; Figure 1 2 The figure shows the operator interface of the production rate controller; Figure 13 shows the control screen provided to the engineer interface; Figure 14 shows the production speed within the cooling constraint variable in Example 1 Maximized results; This paper size applies the Chinese National Standard (CNS) Α4 specification (210 × 297 mm) -20-523647 Α7 Β7 Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs 5. Description of the invention (Figure 1) The results of the optimized production rate by the production rate controller in Example 2; Figure 16 shows the results of Example 3, where the production rate is a function of the amount of catalyst in the reactor and the cooling water △ T; Figure 17 shows The results of Comparative Example 1 show the potential importance of adjusting the dew point. DESCRIPTION OF SYMBOLS 10 Reactor 12 Reaction zone 14 Reaction deceleration zone 16 Catalyst feeder 2 1 Gas analyzer 2 2 Circulation pipe 2 4 Heat exchanger 2 8 Gas distribution plate 5 2 Metering plate 7 0 Cooling water valve 8 0 First Cooling water pump 8 2 Second cooling water pump 10 0 Speed controller 12 0 Operator interface 13 0 Catalyst feeder balance controller 14 〇 Feeder startup initialization control logic (Please read the precautions on the back before filling this page) This paper size applies to Chinese National Standard (CNS) A4 specifications (210 × 297 mm) -21-523647 Α7 Β7 V. Description of the invention (15 0 R Ρ Μ Ρ ID controller (please read the precautions on the back before filling this page) 160 Cooling potential loss alarm 17 0 CWDT deviation from high priority alarm 180 CW pump logic control 2 0 0 low signal selector 2 12 PD production rate controller 222 PID purge tank water level controller 2 3 2 PD ID condensate Weight percentage controller 2 4 2 PD valve position controller 2 4 6 PD ID cooling water △ T controller 260 calculation logic controller 262 low signal selector 2 9 0 catalyst R Ρ Μ control The detailed description of the device is printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs. In order to illustrate the specific examples of the present invention, the following describes the details of the present invention through examples to provide the present invention that is considered to be the most useful and easy to understand. Principles and conceptual aspects. Therefore, the details beyond the basic understanding of the present invention will not be described, and the description made with reference to the chart enables those skilled in the art to easily understand that the various forms of the present invention are put into practical use. All measured quantities in the following description, unless otherwise specified, refer to the weight percentage of a given sample. Thus, for example, 30% means 30% of the weight ratio of the sample.- 22- This paper size applies Chinese National Standard (CNS) A4 specification (210 × 297 mm) 523647 A7 B7 V. Description of the invention (2¾ (Please read the notes on the back before filling this page) Unless otherwise specified, the following mentioned A compound or an ingredient refers not only to the compound or the ingredient itself, but also to mixtures formed with other compounds or ingredients. Generally speaking, the present invention relates to a system and method for controlling the catalyst feed rate based on one or more constraint variables. Although the catalyst feed rate can be controlled by only one variable, a multi-variable system can usually obtain a comparative Good results. Constraints can include reaction conditions, such as required production rate, effective heat transfer (such as cooling water ΔT, cooling water valve position), dew point boundary, weight percent condensate, weight percent condensable, product Removal (such as purge tank water level), degree of fluidization, degree of entrainment, spherical 'granular resin transmission rate, and / or raw material addition (such as raw material pressure). The present invention can be used to control reactions that can control the reaction rate by changing the catalyst feed rate. Therefore, the method of the present invention can be applied to almost all reactors. The invention is suitable for both endothermic and exothermic reaction processes. Examples of the reaction of the present invention include catalytic cracking and gas phase polymerization in a fluidized bed. Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs. However, the present invention is a better example for controlling the exothermic polymerization reaction of a fluidized bed. Generally speaking, the preparation of resin materials in a fluidized bed process, especially the process of preparing polymers from polymerized monomers, usually involves continuously passing a gas stream containing one or more monomers through the fluidization under the reaction conditions and the presence of a catalyst. Bed reactor. The gas stream containing unreacted gaseous monomer is continuously withdrawn from the reactor, compressed, cooled and recycled into the reactor. The product is separated from the reactor. Add additional reaction monomers, such as to the circulating gas stream. -23- This paper size applies to China National Standard (CNS) A4 specification (2 丨 〇 > < 297 mm) 523647 A7 B7 V. Description of the invention (2) (Please read the precautions on the back before filling out this page) The polymerization reaction is exothermic, so the temperature of the gas flow in the reactor should The decomposition temperature of the media is lower than the melting temperature and the viscosity temperature of the resin particles generated during the polymerization reaction. Such temperature control is necessary to prevent blockage of the reactor caused by the rapidly growing polymer mass that cannot be continuously removed from the reactor as a product. Therefore, it can be considered that the amount of polymer produced within a given time in a fluidized bed reactor of a given volume is directly related to the amount of heat removed from the fluidized bed reactor. In the following, some constraint variables that limit the production rate will be described in more detail. The present invention is based on the recognition of these constrained variables. These variables include, but are not limited to, the required production rate, effective heat transfer, dew point boundary, weight percent of condensate, product removal (such as purge tank water level), degree of fluidization , Degree of entrainment, granulator, granular resin transmission capacity, and / or raw material addition (such as raw material addition pressure). "Effective heat transfer" as mentioned here refers to the effective cooling capacity in a given time, which can be determined by cooling water △ T (large △ T corresponds to large effective heat transfer) and / or cooling water valve Location decision. Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economics The present invention relates to a method and system for restricting variable override control based on the input of one or more constraint variables to control the production rate by changing the catalyst feed rate. In one aspect, the present invention relates to the required production rate, effective heat transfer, dew point boundary, weight percentage of condensate, weight percentage of condensable, removal of product (such as purge tank water level), degree of fluidization, degree of entrainment, Granulator, granular resin transmission capacity, and / or raw material addition (such as raw material addition pressure), the reaction is automatically changed by changing the catalyst feed rate. The paper size is applicable to the China National Standard (CNS) A4 specification (210X 297). (%) "94 a" 523647 A7 B7 V. Description of the invention (3 Control. (Please read the precautions on the back before filling this page) The invention is also about a system and method that triggers an alarm when the effective heat transfer suddenly changes In addition, the present invention relates to a method and system for controlling the second pump. Proper control of the second pump can make the automatic control of the production rate run optimally and avoid runaway reactions. In order to better understand the advantages of the control system and method of the present invention The following is a non-limiting example of gas phase polymerization. In order to better understand the automatic control of gas phase polymerization in the present invention, The system and method need to have a general understanding of the fluidized bed gas phase polymerization reaction. Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs, although the fluidized bed reactor of the present invention is not limited to some specific reactors' As mentioned above, the reactor of the present invention must be able to operate in dry mode and condensing mode. In general, in the dry mode, the circulating gas stream is cooled above the dew point, so that only the gas phase exists in the circulating gas. In the condensing mode Then, the circulating gas is condensed below the dew point, and a two-phase gas-liquid mixture is formed under certain conditions. In this way, at least at the entrance of the fluidized bed reactor until the liquid phase volatilizes or enters the fluidized bed, the The liquid phase in the mixture is entrained in the gas phase in the mixture. The location of the circulating gas entering the fluidized bed must be below the fluidized bed (polymerization zone) to ensure the uniformity of the upstream gas flow and the suspended state of the bed. The location of entry into the fluidized bed is generally in the lower position of the reactor, preferably the bottom of the reactor, to ensure the uniformity of the upstream fluid passing through the fluidized bed. Place a baffle or similar device near the inlet of the circulating gas for -25-This paper size applies Chinese National Standard (CNS) A4 (210X297 mm) 523647 A7 B7 V. Description of the invention (2¾ Prevent low air velocity Zone, so that solid and gaseous materials will remain in the upstream circulating airflow. (Please read the precautions on the back before filling this page) The circulating airflow can be divided into two and multiple airflows, one or more of which is directly The polymerization zone is introduced so that it has a sufficient gas velocity under and through the fluidized bed to maintain the suspended state of the fluidized bed. In all cases, the 'circulation heat' must keep its composition strictly consistent and uniform, and its flow The form must be such that there is no dead angle in the reactor that generates non-removable solid materials. Injecting the compensation polymerization monomer into the reactor in the form of liquid and / or solid can obtain better results. The present invention discusses a method for compensating the polymerized monomer in the gas phase or the liquid phase at the inlet of the recycle gas or elsewhere in the reactor or in the recycle gas stream. Figure 2 is a non-limiting example of the invention. First of all, it must be pointed out that the process of the present invention is not limited to some specific equipment or pipeline layout. For example, each device shown in a specific example of the present invention may be a plurality of groups of multi-level or parallel devices. Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs. Figure 2 shows a fluidized bed reactor designed according to the present invention, which is particularly suitable for the production of polyolefin resin. In the second figure, T I = temperature indicator, TC = temperature controller, 〇 = output, SP = selected 値 'SC = speed controller, pv = process variable. The reactor 10 includes a reaction zone 12 and a deceleration zone 14. In general, the preferred range of height and diameter ratio of the reaction zone is from 2. 7: 1 to 5: 1. Of course, this range can be made larger or smaller depending on the required production capacity. Generally speaking, the cross section of the deceleration zone 1 4 is the same as the Chinese standard (CNS) A4 specification (210X 297 mm). _ 26 _ 523647 A7 B7 V. Description of the invention (d Cross section of the reaction zone 1 2 The area is about 2. 6 to 2. 8 times. The reaction zone 12 includes a polymer particle growth bed, a continuous flow of gas and circulating gas of polymerizable and adjusted gaseous components in the form of compensating raw materials formed by the polymer particles and a small amount of catalyst particles through the reaction zone. Under the effect of fluidization on the bed. In order to maintain a suitable fluidized bed, the surface gas velocity through the bed must be higher than the minimum flow velocity required for fluidization, and the preferred surface gas velocity must be at least about 0.2 ft / s above the minimum flow velocity required for fluidization. Generally speaking, the surface air velocity is not higher than 5 · 〇 f t / s, usually 2. 5 f t / s is sufficient. It is important that the fluidized bed always contains certain particles to prevent the formation of local "hot spots" and to introduce and disperse a specific catalyst throughout the reaction zone. Initially, a specific polymeric matrix material is usually added to the reactor before the gas stream is introduced. These particles may be the same as or different from the polymer to be synthesized. When it is different from the synthetic product, they flow out of the reactor together with the synthesized polymer as a preliminary product. Finally, a fluidized bed of synthetic polymer particles is required to replace the initial fluidized bed. Partially or fully activated raw materials and / or catalysts in the fluidized bed are preferably stored in the memory 16 for use, for example, one or more catalyst feeders 16 controlled by the speed controller SC The material is in an inert protective atmosphere such as nitrogen or argon. As will be described in further detail below, the memory preferably includes two catalyst feeders. The fluidization state is achieved through high-speed fluid circulation and through the bed, which is generally to compensate 20 to 70 times the flow rate of the raw material stream, usually 30 to 60 times, and most commonly 40 times. The general morphology of the fluidized bed is immersed in this paper. The standard of China National Standards (CNS) A4 (210X297 mm) is applicable (please read the notes on the back before filling this page). Printed by the cooperative 523647 A7 _____ B7 V. Description of the invention (2) (please read the precautions on the back before filling this page) The densely moving particles of the gas flowing through the reactor. Cross-section divided fluid bed weight. Thus, the pressure drop depends on the geometry of the reactor. The compensation fluid is injected into the fluid bed at positions 18. The composition of the compensation fluid is determined by a gas analyzer. Gas analyzer 2 1 Determine the composition of the circulating gas and adjust the composition of the compensation fluid according to the measurement to maintain a stable gas phase composition in the reaction zone. There are a large number of commercially available gas analyzers. Generally speaking, the gas analyzer is placed to be able to analyze the deceleration zone Position of the gas between 1 4 and the heat transfer zone 24. To ensure complete fluidization, the circulating flow and, if necessary, part of the compensating air flow via the circulation tube 2 2 in The 2 and 6 positions below the layer are refluxed into the reactor. A dispersion plate is added above the reflux position to assist in the bed fluidization. The circulating gas passes the fluidized bed and absorbs the reaction heat generated by the polymerization reaction. After leaving the polymerization zone, the part of the fluid that constitutes the circulating gas that does not react on the fluidized bed is preferably passed through a deceleration zone so that the solid particles in it can fall back to the fluidized bed. Wisdom of the Ministry of Economic Affairs Printed by the Property Cooperative Consumer Cooperative and the circulating gas is compressed in a compressor 30 and then passed through a heat transfer zone where the reaction heat is exchanged before the recycle gas returns to the fluidized bed. The heat transfer zone is generally a heat exchanger 24, such as horizontal or vertical. Then, the circulating gas flow returns to the reactor at the bottom of the reactor 26 and enters the fluidized bed through the gas distribution plate 28. A gas conversion device is usually installed in the reactor. At the entrance, prevent the polymer particles from flowing out or agglomerate. -28- This paper size applies to China National Standard (CNS) A4 specification (210 × 297 mm) 523647 A7 B7 V. Description of the invention (2) (Please read the notes on the back before filling this page) In a stable state, the temperature of the fluidized bed is controlled to a fixed temperature by frequently removing the reaction heat. In a fluidized bed There is no obvious temperature gradient in the upper part. The temperature gradient generally exists in the interval between the temperature of the inlet fluid at the bottom of the fluidized bed and the residue on the bed, which is generally 48 feet high (1. 2 meters), especially 24 feet (6 lcm), and more commonly at 12 feet (30 cm). The temperature gradient is typically up to about 50 ° C, more typically up to about 30 ° C, and a typical range is about 10-20 ° C. Good gas dispersion plays an important role in the operation of the reactor. The fluidized bed contains growing and formed polymer particles, and catalyst particles. Because the polymer particles are hot and may still be active, they must be avoided from standing still, because once there is a static mass, the activated catalyst in it will react further, causing it to melt. Therefore, it is important to keep the circulating gas flow through the fluidized bed at a sufficiently high speed to maintain its fluidized state. Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs. Gas distribution board 28 is a kind of equipment to obtain good gas distribution effect. It can be a screen, trough plate, perforated plate, blister-shaped plate, etc. All components of the board may be fixed or a movable board as described in U.S. Patent No. 3,298,792 to Di DRU SCO, the disclosure of which is incorporated herein by reference. Regardless of the design, the gas distribution plate is used to disperse the circulating gas so that it can pass through the particles at the bottom of the fluidized bed to keep the fluidized bed fluidized while maintaining a stable bed of resin particles when the reactor is not running. Any kind of fluid that is inert to catalysts and reactants can be used in accordance with Chinese paper standard (CNS) A4 (210 X 297 mm) according to this paper standard. _ 29 _ 523647 A7 B7 Specific examples include saturated hydrocarbons, such as alkanes, such as isopentane, n-pentane, isohexane, and n-hexane. (Please read the notes on the back before filling this page) If you use one or more catalysts, such as one or more The co-catalyst can be added to the reaction system from the heat exchanger 24 to obtain a better effect. In this way, the 'catalyst can be injected into the reaction system via the pipe 40 through the disperser. A typical co-catalyst is the Academy Foundation, such as Triethyl, trimethylaluminum (tma), tributylaluminum, methylalumoxane (ma0), etc. Such catalysts can be used in Ziegler-Natta reactions and metallocenes Catalytic system. Fluidized bed reactors are best operated below the sintering temperature of polymer particles to ensure that sintering does not occur. Sintering temperature is a function of the density of the resin material. For example, in general, the sintering temperature of low density resin polyethylene low , And high-density polyethylene resin has a higher sintering temperature. For example, the temperature range is 7 5 ° C-95 ° C is suitable for the production density range of about 0. 9 1 to 0. 95g / cm3 of ethylene copolymer, and the temperature range of 100-115 ° C is suitable for the production density range. 95 — 0. 97 g / c m3 of ethylene storage copolymer. Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs. Fluidized bed reactors can work under pressures exceeding 1000 p s i (6.9 Mpa). For polyolefin products, the working pressure of the reactor is about 100-400 psi (0. 69 to 2. 8 M p a), a better working pressure is 200-400 ps i (1 · 4-2 · 8 M p a), and the best is about 250-350 psi (1. 7-2. 4 M pa), which is conducive to heat transmission under such high pressure conditions, because the pressure increase can increase the single -30- This paper size applies the Chinese National Standard (CNS) A4 specification (210 '乂 297 mm) 523647 A7 B7 V. Description of the invention (heat capacity of 2¾-position volume gas. As mentioned in the background of the invention, when the dew point of the circulating gas needs to be increased, the working pressure can be increased. (Please read the precautions on the back before filling this page) Wisdom of the Ministry of Economy The property bureau employee consumer cooperative prints partially activated or fully activated raw materials and / or catalysts (hereinafter, all are simply referred to as catalysts) into the catheter 4 2 or may be at the 4 4 position on the diffuser 28 The rate of consumption is injected into the reaction bed. Preferably, the position where the catalyst is injected into the reactor can meet the well-mixed polymer. Adding the catalyst above the disperser can better meet the requirements of the fluidized bed polymerization reactor. Work requirements. Because the catalyst is highly activated, injecting the catalyst at a position below the disperser will cause the polymerization reaction to occur there, and eventually lead to the clogging of the disperser. In addition, in the Injecting the catalyst above the diffuser can help the catalyst to disperse on the reaction bed, avoiding the local concentration being too high due to the high catalyst concentration, forming a "hot spot". Injecting the catalyst above the reaction bed will cause too much catalyst Into the circulation pipeline, the polymerization reaction occurs in it, the pipeline is blocked, and finally the heat exchanger is blocked. Therefore, the position of the catalyst injection reactor is generally located at 10-50% from the reactor wall reactor diameter. It is 15-40%, preferably 20-35%, and its height is about 5-30% of the height of the reaction bed, preferably 5-25%, and most preferably 5-15%. Various techniques can be used to inject the reactor into the reactor. However, the better effect is the method of continuous injection of the catalyst in the US Patent No. 3,779,712 to CALVERT et al., The disclosure of which is incorporated herein by reference. Figure 3 shows the catalyst feeder 16 that can be used according to the method of the present invention. The catalyst feeder 16 is similar to the catalyst feeder described in CALVERT et al. (CNS) A4 size (210X297 mm) 52 3647 A7 B7 V. Description of the invention (2¾ feeder. The difference is that the catalyst feeder 16 includes two fog chambers or blocks 46. (Please read the precautions on the back before filling this page) Figure 4 is a fragmentary cross-sectional view of the catalyst feeder 16. The catalyst is in the lower container 4 8 of the catalyst feeder 16. The lower container. 48 contains two eyes p 0 r t 50. Below the lower container is a flow tray 5 2 with a cavity 5 4. The flow plate 5 2 can be rotated by the rotation handle 5 6. Below the flow pan is a lower wheel 5 with two inlets. Each entrance is connected to a block 4 6 respectively. The function of the catalyst feeder 16 is basically similar to the catalyst feeder described by CALVERT et al. In general, when the flow disk rotates, each cavity 54 through the tube 50 will be filled with catalyst. Then, when the cavity 5 4 filled with the catalyst and the inlet 60 are in a straight line, the catalyst is introduced into the block 46. In this way, the speed of the catalyst 'feed can be controlled by turning the flow dial 52. It is preferred to use a gas inert to the catalyst, such as nitrogen or argon, to bring the catalyst into the reaction bed. Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs The polymer production rate in this bed depends on the catalyst injection rate and the monomer concentration in the circulating gas. However, some constrained variables can affect the maximum response rate 値. Specific constraints include, but are not limited to: cooling water △ temperature (effective endothermic 値), circulating gas dew point, 値 for the maximum allowable inert coolant used to keep the reaction bed well fluidized, and the temperature at which the coolant leaves the reactor rate. The present invention is equally effective for each of the constraint variables described above. As such, the present invention relates to controlling the reaction rate based on one or more of the aforementioned variables. Specific examples of these constrained variables include -32- This paper size applies the Chinese National Standard (CNS) A4 specification (210X297 mm) 523647 Α7 Β7 V. Description of the invention (3ί) (Please read the precautions on the back before filling this page ) Desirable production rate, effective heat transfer, which changes with external conditions (such as cooling water △ T, cooling water valve position, flow rate through the cooling tower), dew point boundary, condensate weight percentage, condensable weight percentage , Product removal (such as purge tank water level), fluidization degree, entrainment degree, granulator, granular resin conveying capacity and feed (such as feed pressure). In gas-phase polymerization, one of the frequently reached constraints is effective cooling. An important means of effective cooling measurement is the temperature difference between the temperature of the cooling water entering the heat exchanger and the initial temperature of the cooling water. The temperature at which the cooling water enters the heat exchanger is referred to as the “mixing point”, which means that the compensation cooling water and circulating water are mixed in the circulating pipe. In order to determine the effective cooling, the following definition of cooling water △ T (CWD Τ) is used: CWD Τ = “mixing point” water temperature-water supply temperature Printed by the employee's consumer cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs When CWD τ approaches zero, it arrives The theoretical upper limit of cooling is reached, for example, when the cooling water valve 70 is fully opened and more than 95% of the water passing through the cooling tower is used in the cooling system shown in FIG. 2. The dynamic relationship between effective cooling and catalyst feed change as determined by C W D T is an important aspect of the design of the production rate controller of the present invention. Fig. 5 is a general diagram showing a non-limiting example of the production rate controller logic of a gas phase polymerization reaction, in which the production constraints include the target production rate, the cooling water △ T, the cooling water valve 70 position, and the dew point. However, the configuration of the control system in the present invention can also be extended to a method capable of achieving the object of the present invention. -33- This paper size applies Chinese National Standard (CNS) A4 specification (210 × 297 mm) 523647 A7 ___ B7___ V. Description of the invention (3) (Please read the precautions on the back before filling this page) In Figure 5, The rate controller preferably includes a calculation program. Therefore, the present invention preferably includes a digital computer for calculating the required control signal based on the measured process parameters and the preset 输入 inputted to the computer. The invention can be used as a part of a distributed control system (DCS). Examples of such systems commercially available according to the present invention include Foxboro IA (Smart Automatic Control) and Honerwell TDC-3000. Other types of control systems can also be used in the present invention. The rate controller 1 0 0 is programmed according to the target production rate 10 2, the target CW Valve Position 1 04 and a target dew point 1 06. In this way, the operator enters in detail the target number 接近 that is close to the limit of the constraint variables such as the production rate, the position of the cooling water valve 70, and the dew point. According to historical data, the speed controller 100 automatically translates the cooling water valve position 104 into a suitable cooling water ΔT close to the limit. The rate controller 1 0 0 compares the measured production rate 1 1 0 with the target 値 and measures the cooling water valve position (CW Valve Position) Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs 1 1 2 and the measured cooling water △ T (CWDT) 1 1 4 is compared, and the measured dew point (DewPt) 1 1 6 is compared with the target 値. The comparison of the cooling water valve position 70 and C W D T includes the cascade logic discussed in detail below. Refer to Figure 7. The rate controller interacts with the operator interface via a signal 1 2 2. The operator interface includes, for example, a monitor and a keyboard. The operator inputs the desired preset via the operator interface 1 2 0. The rate controller is also controlled by the signal 1 2 8 and the catalyst feed balance control system. -34- This paper size is applicable to the Chinese National Standard (CNS) A4 specification (210X297 mm) 523647 A7 _______B7 ___ 5. Description of the invention (d (please first Read the notes on the back and then fill out this page) system interaction. According to the dynamic response signal of the device, the control logic of the catalyst feeder balance controller 1 3 0 calculates the total catalyst R PM optimization target 値 'and then balances the score. To the running catalyst feeder. For example, historical data on the relationship between CWDT and catalyst feed rate can be analyzed to obtain a dynamic response. Commercially available dynamic analysis software such as OH Cincinnai Arton's "PIT0PSTM" can be used to calculate the dynamic transfer function of all constrained variables. Analysis shows that the information on the dynamic change of cooling water △ T is sufficient to determine the process dynamics of the controller. Catalyst feed balance controller 1 3 0 Interaction between the same block and a feeder start initialization control logic 1 4 0 via a signal 1 3 2. Block and feeder start initialization control logic 1 4 0 In order to make the change between manual operation and automatic control smooth, the consumer intellectual property bureau of the Ministry of Economic Affairs, the consumer cooperative prints the block and the feeder starts the initialization control logic 1 4 〇 transmits an RPM signal 1 42 to the RPM PID (proportion one integral- Differential (propertional-integral-derivative) controller 50. The R P M P ID controller 1 5 0 will be the current feeder R ρ μ 1 5 2 and the initialization control logic 1 from the block and feeder start 4 〇 The obtained RP Μ signal is compared, and an r ρ Μ signal 1 5 4 is calculated and transmitted to the motor controlling the catalyst feeder to control the catalyst feed rate. Using the control logic shown in Figure 5, if Need to maximize production rate 'The operator must give a high preset rate of target production rate 104. The controller 100 will increase the RPM of the catalyst feeder until it reaches the boundaries of other preset rates, and then maintain The R Ρ Μ 値. In other words, if the production rate is maximized 'then it is necessary to specify a high standard that cannot be met with this paper. Applicable Chinese National Standard (CNS) A4 specification (210X297 mm) ~-523647 A7 _______ B7_ V. The default description of the description of the invention (3 $ (please read the notes on the back before filling this page). In this way, the catalyst feeder will accelerate to reach the set production rate. When the production rate rises, it is close to other Constrained variable boundaries. Constrained p ID 値 will be lower than the production rate PID; reduce the feed rate of the catalyst into the reactor. For example, a restricted constrained variable is usually effective cooling. For effective cooling, the cooling water method door 70 position and CW D T continuously monitor its dynamics. Figure 5 also shows the cooling potential loss alarm 160. For any reason, if C W D T rises quickly, a high priority alarm 160 will warn the operator. The sudden rise of CWDT may be due to unknown toxic substances in the raw materials, bad catalysts or other reasons that cause the reaction to decay. In this case, it is not desirable to increase the flow rate of the catalyst into the reactor. Alarms can respond to even the operator's problems, alert to check reactor conditions, and take appropriate action including cancelling automatic control. Figure 5 further illustrates a CWD T departure from high priority alarm 170. This high priority alarm gives the operator a potential runaway warning. If the response is suddenly out of control, a rapid increase in the CWDT reduction rate, or a rapid opening of the cooling water valve can trigger an alarm. Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs Figure 6. The reactor cooling system can include a first cooling water pump 80 and a second cooling water pump 82. Figure 5 also shows the CW pump logic control (automatically starting the backup pump) 180. In the event that the first cooling water pump fails, the control logic automatically recommends starting the secondary (standby) pump 8 2. Logic is automatically triggered based on the delta pressure of the running pump 80, the on / off level of the motor, the outflow pressure of the pump, and other possible inputs. If any one of them is input, it means Li-36- This paper size is applicable to Chinese National Standard (CNS) A4 specifications (21 °, 公 297 mm) 523647 A7 B7 V. Description of the invention (If the work fails, the backup pump 8 2 will Automatic start. In this way, under the condition that the reactor is running, the running pump 80 will start when any of the following conditions occur: low △ pressure of pump 80, low motor k W or amps, on-to-off The feedback signal shows that the motor is "not running", and the interruption request detected by the alarm of the distributed control system. In addition, the second pump 82 can be operated at a low speed under normal conditions, and the operating speed of the pump can be increased if the first pump fails. When both pumps cannot operate normally, the logic control will automatically shut down the reactor. Figure 7 is a general diagram of another non-limiting example of the logic controller for the production rate of the gas phase polymerization reaction, where the production constraint variables Including the required production rate, the required purge box water level, the maximum weight percentage of condensate, the maximum position of the cooling water valve 70. At this point, the purge box is the product inlet. Temporary storage place before step processing. In Figure 7, a low-signal selector 2 0 0 selects the lowest of the multiple constraint variables as the constraint variable that restricts production. The low-signal selector 2 0 0 and the low-signal selector Together with the PID controller above the controller 200, the function of the rate controller in Figure 5 is realized, which will be further described below. The selected signal in Figure 7 includes a required production rate 2 2 and a required purge tank water level. 2 0 4. The maximum weight percentage of condensate is 2 0 6 and the maximum position of a permitted cooling water (CW) valve is 2 0 8. The required production rate 2 0 2 and the determined current production rate 2 1 0 are produced in a PID Rate controller (PRAT C) 2 1 2 for comparison, the controller sends the production rate signal 2 1 4 to the basic salary. Good choice --------- 41 ^ — (Please read the precautions on the back before (Fill in this page) Order printed by the Intellectual Property Bureau of the Ministry of Economy ’s Consumer Cooperatives. The paper size is applicable to Chinese National Standards (CNS) A4 specifications {210X297 mm) -37- 523647 Α7 Β7 V. Description of the invention (β (Please read the first (Please fill in this page again) In the reactor 200. The production rate controller (PRATC) 2 12 is reversed (if the production rate (PV) rises, the output 値 must decrease). The output signal 2 1 4 is the total R ρ sent to the reactor The amount of M is expressed by the production rate. The required purge box water level 2 0 4 and the measured purge box water level 2 2 0 are compared in a PID purge box water level controller (PBNLC) 222 which compares a The purge tank water level signal is sent to the low signal selector 200. The purge tank water level controller (PBNLC) 222 is reversed (if the level (PV) rises, the output must decrease). The output signal 2 2 4 is the total amount of RP M fed to the reactor, and is expressed via the purge tank water level. The maximum weight of condensate printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs is 206 and the measured condensate weight percent 2 3 0 is compared in a P ID condensate weight percent controller (WCONC) 2 3 2 The controller phase low signal selector 2 0 0 sends a condensate weight percentage signal 2 3 4. The condensate weight percentage controller (WCOCNC) 2 3 2 is reversed (if the measured condensate weight percentage 230 rises, the output decreases). The output signal 2 3 4 is the total RP M 値 'entering the reactor, expressed as a weight percentage of the condensate. In this regard, the operator sets the maximum condensate weight percentage as a preset for the controller. When the production rate increases or other process conditions change, if it is close to the preset threshold, the logic control automatically adjusts the catalyst RPM to maintain the condensate boundary conditions or make it lower than the preset threshold. Although it is not desired to be limited to experience, most of the time, one usually chooses another constraint variable. This paper scale applies Chinese National Standard (CNS) A4 specification (21〇297297 clock) -38- 523647 A7 — —_ B7 V. Description of the invention (3¾ the maximum allowed cooling water valve position 2 0 8 and a measured cooling water Valve position 2 4 0, which can be the average value of the cooling water valve 70 position. For comparison in the PID valve position controller (VALVC) 2 4 2, the controller sends the valve position signal 2 4 4 to a PID cooling. In the water △ T controller (CWDTC) 2 4 6, the ○ boundary 0 Ding (: the controller simultaneously receives a measured cooling water △ T signal 2 4 8. The valve position controller (VALVC) as a main PID and is directly (If the measured CW valve position (PV) is increased, the output must also be increased). Cooling water △ T controller (CWDTC) 2 4 6 as a servo PID and directly acting (if the measured CWDT is increased, the output is increased Large). The valve position signal 2 4 4 is the total RP M entering the reactor, which is indicated by the cooling water valve position. P ID cooling water △ controller (CWDTC) 2 4 6 will effectively cool the signal 2 50, based on CWD The total R MP feed of T, Into the low signal selector. In this way, the cascade control loop formed by VALVC and CWDTC is used to measure and control the cooling constraint variable. The cooling constraint variable in an exothermic reaction system releases a very important constraint variable, which is generally the most important A constraint variable. All the designs that can improve the control of the constraint variables can directly benefit the maximization of the production rate. The cascade control system will linearize the nonlinear relationship of the 70 parameters of the cooling water valve. Based on observations and experience, it can be determined Beyond the boundary of the 70 position of the CW valve, beyond this boundary, the effective cooling is basically small enough to be ignored. This position can be changed from the CW valve position of 6 5% opening to about 80% opening. Each valve is judged by experience. When the CW valve 70 is connected to this paper, the Chinese national standard (CNS) A4 specification (210 X 297 mm) is used. _ 39-I —------ 衣-(Please read first Note on the back, please fill out this page) Order printed by the Intellectual Property Bureau of the Ministry of Economic Affairs, Consumer Cooperatives 523647 A7 B7 V. Invention Description (3) (Please read the notes on the back before filling this page) Near At its maximum, the master-servo PID joint controller works together to effectively reduce the catalyst feed rate. Using isolated CWDT signals or other variable parameters of the cooling constraint variables, such as the flow rate through the cooling tower, cannot be effectively Complete the same work. Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs Usually, there is a one-to-one relationship between the CW valve 70 position and the CWD T. When the reactor cannot be cooled (the CW valve 70 is in the almost fully open position), the CW D T is at a minimum value (the minimum temperature difference between the saturated steam and the coolant corresponds to no additional cooling). Multi-level control systems including VALVC and CWDTC multi-level points take advantage of this relationship. CWDTC is a linear signal and works better in relatively fast-tuning servo (internal) loops. When the effective cooling decreases, the CWDTC servo effectively reduces its output 値, so that appropriate actions are made accurately. Although CWDTC can make correct actions in a short period of time, in the long run it does not have the ability to really determine the cooling boundary. The cooling boundary can be determined more accurately by averaging the 70 position of the CW valve. This is because the valve position undoubtedly accurately represents the cooling capacity (or lack of). The valve position filter is used in the VALVC controller (and its preset for resetting the CW D T controller) is combined with the signals from both controllers. The combined multi-stage controller knows the exact cooling boundary and responds at the appropriate speed. The VALVC controller cannot be used separately from the CWDTC controller because the valve position signal is highly non-linear, especially when the valve position opening is greater than 75% (the most interesting area from the perspective of maximizing the rate). By adopting these two controllers in a multi-level structure, short-term and long-term goals can be achieved. Therefore, each PID such as 212, 222, 232, -40- This paper standard applies to China National Standard (CNS) A4 specifications ( 210 X 297 mm) 523647 Α7 Β7 V. Description of the invention (d (please read the notes on the back before filling this page) 2 4 6 The output 値 are based on the catalyst feed rate. Therefore, the lowest signal The selector 2 0 0 selects the lowest output 四个 (constrained variable output) of the four PIDs. The lowest signal selector 2 0 0 and a designed computational logic controller 2 6 0 pass the signal 2 6 2, including the four PIDs. The lowest signal 'interaction. The calculation logic controller of this design completes the start and initialization control logic of the catalyst feed balance controller module 130 and the feeder of Fig. 5. The calculation of the design The logic controller 2 60, two catalyst feeders 16 with independent blocks, each bring certain difficulties to the configuration and startup of the control. The specific control logic requires correct startup, local to remote End -PC AS (such as multi-level program)) smoothly converted. In order to maintain clarity and easy maintenance, the entire control logic is divided into four main logic modules, such as RP M start logic, RP M splitter logic, preset値 Processing logic and RPM anti-termination logic. The controller can be implemented in different ways depending on the type of platform. For example, the logic modules shown here can be combined or separated without departing from the scope of the invention. Ministry of Economic Affairs Printed by the Intellectual Property Bureau employee consumer cooperative as shown in Figure 7, the calculated logic controller 2 6 0 receives a feeder 1 on / off signal 2 6 4 and a feeder 2 on / off signal 2 6 6 , A block 1 1 on / off signal 2 6 8, a block 12 2 on / off signal 2 7 0, a block 21 1 on / off signal 2 7 2, and a block 22 on / off signal 274 Feeder 1 on / off signal 2 6 4 and Feeder 2 on / off signal 2 6 6 indicate the switching status of feeders 1 and 2, respectively. Block 1 1 on / off signal 2 6 8 and block -41-The size of this paper is applicable to Chinese National Standard (CNS) A4 specification (210 × 297 mm) 523647 A7 ___B7 Explanation (3¾ (Please read the precautions on the back before filling this page) 1 2 On / off signal 2 7 0 Respectively the two areas in block 4 6 of the first catalyst feeder as shown in Figure 3 The state of the block is active or blocked. Similarly, block 2 1 on / off signal 2 7 2 and block 2 2 on / off signal 2 7 4 represent the second catalyst feeder in Figure 3 respectively. Whether the state of the two blocks of block 4 6 is running or blocked. As disclosed in more detail with reference to FIG. 8, the RPM activation logic of the logic controller 260 enables the controller to achieve a smooth transition between manual and automatic control by the operator. Reference may also be made to the appendix of the present invention, which includes a list of terms for the control logic examples of the present invention. A non-limiting example of a logic controller that enables RP to start as shown in FIG. The scan time of this logic block is generally between 1-60 seconds, preferably 5-30 seconds, and most preferably 15 seconds. Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs In general, the logic block checks whether the catalyst feeders # 1 and # 2 are ready to receive remote presets from extended control operations. When a logic block is on, the feeder motor is running, and the corresponding RP MP ID is in the automatic and remote state and is not activated, the catalyst feeder can receive the remote preset. If the above conditions are met, then the binary output flags (6001 and 8002) are set to YES and NO (0 or 1). Control logic then determines the total number of blocks entering the reactor. When a block is feeding reactors, its status must be "ON" and its corresponding feeder motor is "running". This allows the total number of blocks to be fed to the reactor to be calculated. The total R P MH obtained from all "on" blocks and "running" feeders is calculated and written to R02. If the control scheme does not have a one-42- this paper size applies to the Chinese National Standard (CNS) A4 specification (210X297 mm) 523647 A7 _______B7 V. Description of the invention (Can't switch to On) 'Then R〇0 2 値 (total R ρ μ) is written into R〇〇1. (Please read the precautions on the back before filling this page) R〇0 1 is used to initialize the upstream stream P ID output 値. If the control scheme is in the "ready" state, r 〇〇2 値 will not be copied to R 〇0 1. Carefully refer to Figure 8, the control logic starts at gg] 3 0 0. At 3 0 At two places, the control logic determines whether the block 11 of the first catalyst feeder or the print by the consumer co-operative society of the Intellectual Property Bureau of the Ministry of Economy 12 is on. If both are off, B〇01 値 is on 03 04 No. If 'at least one block is on, at 306, the control logic determines whether the motor of the first catalyst feeder is on. If the motor of the first catalyst feeder is not on, then B 0 〇 1 値 is set to NO at 3 0 4. If the motor of the first catalyst feeder is at 3 〇6 is on. At 308, the position control logic determines whether the r ρ Μ Ρ ID of the first catalyst feeder is in the automatic and remote state and is not activated. If the RPM PI of the first catalyst feeder is The conditions of being in the remote and automatic modes and not being activated are not met. Β 0 〇1 値 is set to NO at 3 〇. If the R ρ Μ Ρ ID of the first catalyst feeder meets the conditions, it is in the remote Terminal and automatic mode and this condition is not activated, then the position 3 boo 1 is YES. At 3 2 0 'the control logic determines whether block 2 1 or 2 2 of the second catalyst feeder is on. If If both are off, b001 値 is negative at 3 2 2. If at least one block is on, at 3 2 4 the control logic determines whether the motor of the second catalyst feeder is on. If The motor of the second catalyst feeder is not turned on, then BOO1 値 is set to negative at 3 2 2. If the motor of the first catalyst feeder is turned on at 3 2 4 at -43- Paper Standards Suitable for Noodles (CNS) A4 Specification (21GX297 Male Sauce) 523647 A7
五、發明説明（ (請先閲讀背面之注意事項再填寫本頁) 3 2 6位置控制邏輯確定第二觸媒進料器的 R Ρ Μ Ρ I D是否處於自動和遠端狀態並且未啓動。如 果第二觸媒進料器的R Ρ Μ Ρ I ϋ未滿足處於遠端和自 動模式及未啓動迫一條件’ Β ◦〇 1値在3 2 2處設爲非 .。如果第二觸媒進料器的R Ρ Μ Ρ I D値在3 2 6符合 條件，即處於遠端和自動模式及未啓動這一條件，那麽 3 2 8位置Β〇〇 1値爲是。 在3 3 0 ，控制邏輯判斷Β〇〇 1或Β〇〇 2是否爲 是。如果二者皆非’那麽Β〇〇 3在3 3 2處爲非。如果 B〇〇 1和B〇〇 2有一爲是，那麽B〇〇 3在3 34爲 是。 在3 4 0處，控制邏輯計算第一觸媒進料器的運行的 block數目。控制邏輯還計算第二觸媒進料器的運行的區塊 數目。由這些計算所得的値，控制邏輯計算得到總的運行 的區塊的數目。控制邏輯同時還計算總的R ρ Μ進料。控 制邏輯進一步將Β ◦ 0 4設爲Β ◦ 〇 3的逆。 經濟部智慧財產局員工消費合作社印製 在3 5 0處，控制邏輯判斷Β 0 〇 4是否爲真。如果 Β〇〇 4不真，在3 6 0位置邏輯退出。如果Β〇〇 4爲 真，那麽在3 5 2位置將R〇0 1設定與R〇〇 2相等， 在360位置退出。 再參考第7圖，邏輯控制器2 6 0的RPM分流邏輯 試圖明顯提高生產速率控制器的自動化和控制的質量。就 這點來說，細粉狀的觸媒在雙馬達驅動的觸媒進料器1 6 的帶動下進入反應器。如上所述，每個觸媒進料器1 6有 本紙張尺度適用中國國家標準（CNS ) A4規格（210 X 297公釐） _ 44 _ 523647 A7 B7_ 五、發明説明（4 (請先閲讀背面之注意事項再填寫本頁) 兩個形式爲區塊4 6的進料點（見第3圖）。如此，一共 有由兩個進料器驅動的區塊。總的觸媒進入反應器的量是 進料點的函數，也就是說，運行的觸媒進料器1 6的數目 乘上打開的區塊4 6的數。 基於第7圖所示的輸入信號，控制邏輯檢查每個觸媒 進料器1 6的控制等級。如果觸媒進料器未準備接受一個 監控設定値，例如，由於補充觸媒切斷進料器或是由於一 個下行進料點堵塞引起的控制邏輯阻斷觸媒進料器，那麽 計算總的R P Μ値，以局部R P Μ或操作者給定r ρ μ的 形式存儲。 將總的R Ρ Μ値（低信號選擇器輸出）減去操作者給 定R Ρ Μ計算得到“自動”模式的R Ρ Μ値（可以爲速率 控制方案所操縱的R Ρ Μ )。 控制邏輯計算總的準備接受來自速率控制方案的遠端 給定値的區塊的數目。這些準備好的區塊的數目就是自動 區塊的數目。 經濟部智慧財產局員工消費合作社印製 將總的自動R Ρ Μ的値除以總的自動區塊的數目得到 R Ρ Μ控制器之給定値。 如果進料器沒有準備接受一個遠端給定値（例如，因 爲進料器處於手動、近程或啓動狀態），那麽給定値將不 予下傳。而給定値等於由操作者給定的現時的 R Ρ Μ Ρ I D給定値。如果兩個進料器都處於近程模式 (不是遠端模式），那麽控制邏輯將所有區塊的總的 R Ρ Μ値相加，將得到的數値寫入低信號選擇器的輸出。 本紙張尺度適用中國國家標準（CNS ) Α4規格（210X297公釐） 523647 A7 B7 五、發明説明（4¾ 第9圖中所示的是R P Μ分流邏輯的非限制性實例。 該邏輯塊的掃描時間一般約爲1 - 6 0秒，較佳的是5 -3 0秒，最佳的是1 5秒。一般而言，第9圖中的邏輯控 制包括一種每個進料器的R Ρ Μ ρ I D等級檢測器。 詳細參照第9圖，邏輯始於0 0。在4 0 2處 ，如果該進料器RPM Ρ I D處於近程或手動模式，那 麽R Ρ Μ Ρ I D的給定値乘以運行區塊的數目得到的値 存儲爲近程 RPM (在操作者控制下的RPM)。進料 器#1的値存爲Μ01，進料器#2値存爲Μ02。兩値 相加得到處於近程/手動模式下的總的R Ρ Μ値，存爲 R〇0 2。該値稱爲操作者R Ρ Μ。操作者R Ρ Μ從總的 R Ρ M ( low selector tag輸出値）計算得處於自動模式下 得R Ρ Μ値（速率控制系統控制的R Ρ Μ )。該値存爲 R〇01 ，稱之爲自動RPM。計算得到處於自動和遠端 模式下的總的區塊（準備接收來自速率控制系統的遠端給 定値的區塊）數目。該値存爲I 0 0 1 ，就是自動區塊的 數目。 在4 0 4，控制邏輯判斷I 〇 0 1是否非零。如果 I〇0 1非零，也就是說，至少有一個遠端控制區塊，那 麽，在4 0 6，總的自動R Ρ Μ除以自動區塊數目計算出 # 1和# 2速率一變化R Ρ Μ限制區塊2 8 0的給定値， 該給定値經由信號7 8傳送給速率-變化限制模組2 8 0 (見第6圖）。這些模組2 8 0的輸出値2 8 2構成伺服 RPM PID290的給定値。 (請先閱讀背面之注意事項再填寫本頁) 、1V. Description of the invention ((Please read the precautions on the back before filling this page) 3 2 6 The position control logic determines whether the R CMP ID of the second catalyst feeder is in the automatic and remote state and has not been started. If The second catalyst feeder's R Ρ Ρ Ρ ϋ does not meet the conditions of being in remote and automatic mode and not activated. Β ◦〇1 値 is set to 3 at 2 2... If the second catalyst feed The R RP ID of the feeder meets the conditions at 3 2 6, that is, it is in the remote and automatic mode and the condition is not activated, then the 3 2 8 position 〇〇〇1 is YES. At 3 3 0, the control logic Determine whether BOO1 or BOO2 is true. If neither is true, then B003 is false at 32. If B001 and B002 are yes, then B〇 〇3 is 3 at 34. At 3 40, the control logic calculates the number of blocks that the first catalyst feeder runs. The control logic also calculates the number of blocks that the second catalyst feeder runs. From these Calculated 値, the control logic calculates the total number of running blocks. The control logic also calculates the total R ρ M feed. The control logic further sets B ◦ 04 as the inverse of B ◦ 〇3. The employee consumer cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs prints it at 3 50, and the control logic determines whether Β 0 〇4 is true. If Β〇〇4 does not If true, the logic exits at position 360. If B〇〇4 is true, then set R0 01 to be equal to R002 at position 3 52 and exit at position 360. Refer to Figure 7 again for logic control The RPM shunt logic of the device 2 60 attempts to significantly improve the quality of the automation and control of the production rate controller. In this regard, the fine powder catalyst is driven by the dual-motor-driven catalyst feeder 16 Reactor. As mentioned above, each catalyst feeder 16 has the paper size applicable to the Chinese National Standard (CNS) A4 specification (210 X 297 mm) _ 44 _ 523647 A7 B7_ V. Description of the invention (4 (Please Read the notes on the back before filling this page.) The two feed points in the form of block 4 6 (see Figure 3). In this way, there are a total of two blocks driven by the feeder. The total catalyst enters The volume of the reactor is a function of the feed point, that is, Multiply the number of open blocks 4 to 6. Based on the input signal shown in Figure 7, the control logic checks the control level of each catalyst feeder 16. If the catalyst feeder is not ready to accept a monitoring setting例如 For example, if the catalyst feeder is blocked due to supplementary catalyst cut-off feeder or control logic caused by a blockage of a downward feed point, then the total RP Μ 値 is calculated as the local RP Μ or the operator gives It is stored as r ρ μ. Subtract the total RP Μ 値 (low signal selector output) from the operator's given RP Μ to calculate the RP Μ 値 in "automatic" mode (which can be manipulated by the rate control scheme R P M). The control logic calculates the total number of blocks ready to accept a given frame from the far end of the rate control scheme. The number of these prepared blocks is the number of automatic blocks. Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs. Divide the total automatic RP by the total number of automatic blocks to get the given value of the RP 控制器 controller. If the feeder is not ready to accept a remote setpoint (for example, because the feeder is in manual, short range, or activated), then the setpoint will not be downloaded. And the given value is equal to the current R P M P ID given by the operator. If both feeders are in the short range mode (not the remote mode), the control logic adds the total RP M of all blocks and writes the resulting number to the output of the low signal selector. This paper size applies the Chinese National Standard (CNS) A4 specification (210X297 mm) 523647 A7 B7 V. Description of the invention (4¾ Figure 9 shows a non-limiting example of the RPM shunt logic. The scan time of the logic block Generally about 1-60 seconds, preferably 5-30 seconds, and most preferably 15 seconds. In general, the logic control in Fig. 9 includes a kind of RP Μ ρ per feeder ID level detector. Refer to Figure 9 for details. Logic starts at 0 0. At 402, if the feeder RPM P ID is in short-range or manual mode, then the given value of R P M P ID is multiplied by the operation The volume obtained by the number of blocks is stored as a short-range RPM (RPM under the control of the operator). The volume of feeder # 1 is stored as M01, and the volume of feeder # 2 is stored as M02. Adding the two frames results in a short range / The total R P Μ 値 in the manual mode is stored as R0 02. This is called the operator R P M. The operator R P M is calculated from the total R P M (low selector tag output). In the automatic mode, RP Μ 値 (RP Μ controlled by the rate control system) is obtained. This data is stored as 〇01, which is called automatic RPM. Calculated The total number of blocks (ready to receive a block from a remote given frame of the rate control system) in automatic and remote mode. This frame is stored as I 0 0 1, which is the number of automatic blocks. At 4 0 4 The control logic determines whether I 0 0 1 is non-zero. If I 0 0 1 is non-zero, that is, there is at least one remote control block, then, at 406, the total automatic RP Μ divided by the automatic area The number of blocks calculates a given rate of # 1 and # 2 rate-change R P M limit block 2 80, which is transmitted to the rate-change limit module 2 8 0 via a signal 7 8 (see FIG. 6). The output of these modules 2 8 0 値 2 8 2 constitute the setting of servo RPM PID 290. (Please read the precautions on the back before filling this page), 1
T 經濟部智慧財產局員工消費合作社印製 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） _ 46 - 523647 Α7 Β7 五、發明説明（ (請先閲讀背面之注意事項再填寫本頁) 在4 0 8，如果第一觸媒進料器由於某些原因（手動 、近程或啓動狀態）沒有準備接收一個遠端給定値，那麽 該預設値不會下傳至速率變化模組2 8 0。而且，在 4 1 0處，下傳的給定値將被設爲現時操作者給出的 R Ρ Μ Ρ I D預設値。 類似的，在4 1 2處如果第一觸媒進料器由於某些原 因（手動、近程或啓動狀態）沒有準備接收一個遠端給定 値，那麽該預設値不會下傳至速率變化模組2 8 0。而且 ，在4 1 4處，下傳的給定値將被設爲現時操作者給出的 RPM PID預設値。邏輯在416位置退出。 R Ρ Μ 分流邏輯明顯的提高了自動化水平並且方便 了室內操作控制。當速率控制器啓動時，上級控制器在彼 等的給定値與製程條件的基礎上產生R Ρ Μ。該R Ρ Μ分 流邏輯進一步將總的R Ρ Μ値分爲每個區塊需要的R Ρ Μ 値。由於任何情況下，產生的總的R Ρ Μ都是嚴格維持的 ，因此控制的穩定性得到明顯的提高。 經濟部智慧財產局員工消費合作社印製 再次參考第7圖，邏輯控制器2 6 0的給定値處理邏 輯經由保證給定値的平穩變化實現手動到自動控制的平穩 轉換。 就這點來說，如果上游Ρ I D V A L V C 242 ，WC〇NC 232，PRATC 212 和 Ρ B N L C 2 2 2都經由給定値跟蹤啓動給定，那麽當 這些Ρ I D處於啓動狀態（當伺服R Ρ Μ Ρ I D都不準 備接收遠端給定値時），這些上游Ρ I D的給定値等於彼 -47 - 本紙張尺度適用中國國家標準（CNS ) Α4規格（210X297公釐） 523647 A7 _B7___ 五、發明説明（扃 等相應的現時測定値。如此的情況是不好的，因爲當控制 系統啓動時，這些ρ 1 〇的所有給定値都需要存儲和恢復 (請先閲讀背面之注意事項再填寫本頁) 〇 如果配置設置爲沒有給定値跟蹤，那麽給定値將依據 最後登錄値存儲，但是如果給定値與現時測定値之間的差 値較大，也是不利的。 五個上游 P ID VALVC、PRATC、 WCONC、PBNLC和CWDT都必須設置爲給定値 跟蹤啓動。四個P ID VALVC、PRATC、 WCONC、PBNLC還必須設置一個給定値改變速率 限制。 上述的兩個例子的缺點都可以經由增加一個給定値處 理邏輯來克服。第1 0圖中示出了一個給定値處理邏輯的 非限制性實例。該邏輯塊運行的掃描時間一般約爲1 -6 0秒，較佳的約爲5 - 3 0秒，最佳的約爲1 5秒。 經濟部智慧財產局員工消費合作社印製 該邏輯起始於5 0 0。在5 0 2處，該邏輯判斷冷卻 水位置PID (VALVC) 242是否處於手動或自動 狀態，其是否處於近程或遠端狀態，以及其是否啓動。如 果V A L V C 2 4 2狀態爲自動，遠端和未啓動，那麽 504處，VALVC 242的給定値設定爲閥位置的 可允許的最大値。如果V A L V C狀態爲手動或近程或啓 動，那麽506處，VALVC242的給定値爲現時的 冷卻冰閥位置。 在5 0 8，邏輯判斷冷凝物重量百分比（WCONC) -48- 本紙張尺度適用中國國家標準（CNS ) A4規格（210X 297公釐） 523647 A7 _B7_ ____ 五、發明説明（4έ (請先閲讀背面之注意事項再填寫本頁) 232是否處於手動或自動狀態，WCONC 232是 否處於近程或遠端狀態，W C Ο N C 2 3 2是否啓動。 如果WCONC 2 3 2狀態爲自動、遠端並且未啓動， 那麽在510位置，WCONC 232的給定値設定爲 可允許的冷凝物最大百分比。如果W C Ο N C 2 3 2狀 態是手動或近程或啓動 ，那麽在5 1 2位置’ WCONC 2 3 2的給定値爲現時的冷凝物重量百分比 〇 在5 1 4，邏輯判斷生產速率P I D ( PRATC) 212是否處於手動或自動狀態，PRATC 212是 否處於近程或遠端狀態，P R A T C 2 1 2是否啓動。 如果PRATC 212狀態爲自動、遠端並且未啓動， 那麽在5 1 6位置，PRATC 2 1 2的給定値設定爲 所須生產速率。如果P R A T C 2 1 2狀態是手動或近 程或啓動 ，那麽在518位置，WCONC 232的 給定値爲現時的生產速率。 經濟部智慧財產局員工消費合作社印製 在5 2 0，邏輯判斷吹掃箱水位P I D ( PBNLC) 222是否處於手動或自動狀態，PBNLC 222是 否處於近程或遠端狀態，P B N L C 2 2 2是否啓動。 如果PBNLC 222狀態爲自動、遠端並且未啓動， 那麽在522位置，PBNLC 222的給定値設定爲 吹掃箱水位給定値。如果P B N L C 2 2 2狀態是手動 或近程或啓動，那麽在524位置，PBNLC 222 的給定値爲現時的吹掃箱水位。邏輯在5 2 6位置退出。 -49- 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） 523647 Α7 Β7 五、發明説明（ 採用該邏輯和標準給定値跟蹤設計，當速率控制系統 啓動時’所有的上游給定値由彼等的開始値向目標値步進 。如此’所有給定値都是以其相應的最終値存儲的。同時 ’當系統啓動時，由於給定値與實際測定値之間大的偏離 而造成的觸媒進料器中R ρ Μ的大的突變得到避免。 再參考第7圖，RPM防終止邏輯控制器2 6 0可以 使自動控制維持在觸媒進料器的機械性能極限範圍內，如 ，最大觸媒進料速率。 該R Ρ Μ防-終止邏輯在少數區塊運行的情況下能夠 保護防止系統終止。例如，如果四個區塊都以 5 0 0 R Ρ Μ運轉，那麽反應器的總的R Ρ Μ就是 2 0 0 〇。如果三個區塊停轉，單獨運行的區塊將會步進 至最大RPM邊界，也就是說約1 6 0 ORPM。在這種 情況下，速率控制器要求2 0 0 ORPM，但是只有 1 6 0 0 RPM。那麼，生產速率的損失就是不可避免的 。在這種情況下，控制邏輯凍結了上游Ρ I D的內部終止 。否則，上游Ρ I D就會緩慢的保持提阔其輸出値，而控 制器不知道無法達到其餘的那部分R Ρ Μ。 第1 1圖中示出了 R Ρ Μ防終止邏輯的非限制性實例 。該邏輯塊的運行掃描時間一般爲1 — 6 〇秒，較佳的是 5 - 3 0秒，最好是1 5秒。 在600處，邏輯開始。在602處，r〇〇2的値 是運.行的block和進料器的總的R Ρ Μ ’加上的1 〇是作爲 與低信號選擇器輸出値比較的容忍量。在6 〇 4處，邏輯 本紙張尺度適用中國國家標準（CNS ) Α4規格（210X297公釐） -5〇 · I--------衣-- (請先閲讀背面之注意事項再填寫本頁) 訂 經濟部智慧財產局員工消費合作社印製 523647 Α7 Β7 五、發明説明（扃 (請先閱讀背面之注意事項再填寫本頁) 判斷R 0 0 2値是否比低信號選擇器輸出値2 6 2小。如 果R〇0 2不小於其輸出値2 6 2，那麽在6 0 6處， B〇〇1設置爲非真，在處，輸入給上游pID反 饋參數的R P Μ値（以防止終止）設爲等於低信號選擇器 .的輸出値2 6 2 ，邏輯在6 1 0處退出。如果R〇〇 2小 於其輸出値2 6 2，那麽在6 1 2處，邏輯判斷Β 0 0 1 是否爲真。如果Β〇0 1爲真，邏輯在6 1 0處退出。如 果ΒΟ 01非真，β〇〇1在614處設爲真，輸入給上 游Ρ I D反饋參數的r ρ μ値（以防止終止）設爲等於低 信號選擇器的輸出値262，邏輯在610退出。 因爲在6 0 2加上了數値1 〇，如果總的進入反應器 的R Ρ Μ値與低信號選擇器的輸出値之間的差値大於 1 0 R Ρ Μ (容忍量），該終止保護啓動。 一般而言，低信號選擇器的輸出値和總的進入反應器 的R Ρ Μ値相等，並且標記Β〇〇 1 (內部使用僅作顯示 用途）設置爲非真。在這種正常狀態下，上游Ρ I D的反 饋値設爲與低信號選擇器的輸出値相等。 經濟部智慧財產局員工消費合作社印製 當終止條件爲真，標記Β〇〇 1設爲真。只要條件保 持爲真，反饋信號設爲等於最後存儲的低信號選擇器的輸 出値。如此防止了終止。 RPM啓動邏輯，RPM分流邏輯，給定値處理邏輯 和R Ρ Μ防終止邏輯順序或平行工作。較佳的是平行工作 〇 再參照第7圖，如上所述，設計的計算邏輯2 6 0的 -51 - 本紙張尺度適用中國國家標準（CNS ) Α4規格（X297公釐） 523647 A7 ——_B7__ 五、發明説明（扃 (請先閲讀背面之注意事項再填寫本頁) 信號2 7 8送到速率一變化限制塊2 8 0。該速率-變化 限制塊2 8 0解決不能忍受突變的裝置的機械限制問題。 速率一變化限制塊2 8 0將信號2 8 2送到觸媒R P Μ控 制器2 9 0。該R Ρ Μ控制器將所須的速率與實際速率相 比較，調節觸媒進料器馬達的安培數，由此調節觸媒進料 器1 6的進料速率。 第1 2圖是生產速率控制器操作者介面的非限制性實 例。只有三種操作專案供操作者選擇： 1 ·輸入所須生產速率給定値。如果速率需要最大化 ’那麽需要設定一個高的無法達到的數値，如5 0噸/小 時（907千克/小時）。 2 ·指定吹掃箱水位給定値。一般而言，沒有太多必 要改變該給定値。 3 ·啓動速率控制器，將一個或兩個進料器設置爲自 動和遠端模式。如果一個進料器是處於自動和遠端模式的 ’那麽速率控制器開始調節其R Ρ Μ給定値而另一個進料 器R Ρ Μ爲定値。 經濟部智慧財產局員工消費合作社印製 要取消速率控制，那麽兩個進料器都要設定爲近程模 式。一旦給定了合適的給定値，將速率控制器打開，只要 將一個或兩個儘量其由近程模式切換到遠端模式，反之亦 然。不需要其他的操作。 第1 3圖是一個提供給工程師介面的一個單獨的控制 顯示幕的非限制性實例。該顯示幕爲檢查控制表現和確保 控制器各方面運作良好提供了更多的資訊。所有的詳細的 本紙張尺度適用中國國家標準（CNS ) Α4規格（21〇χ297公釐） -52- 523647 A7 B7 五、發明説明（ (請先閱讀背面之注意事項再填寫本頁) 資訊都在該螢幕上給出。該顯示幕使得操作者介面只提供 操作者必須的資訊保持簡潔。如此的安排可以在訓練新操 作員時避免混亂，使所有的操作和理解變的容易且便捷。 在任意一個給出的情況中，低信號選擇器選出四個輸 出値的最低者。選出値著重標記爲方框，如第1 3圖所示 。在這一點上，冷卻水閥位置平均値和平均CWDT是幫 助工程師確定生產速率是否被最大化的很重要的指標。較 佳的是顯示一個2 0或3 0分鐘的平均値。 五個P ID控制器PRATC，PBNLC， WCONC，CWDTC，VALVC必須使用一種工業 製程控制套裝軟體準確調試。例如，如上所述，辛辛那提 俄亥俄州的Artcon公司生產的PITOPSTM軟體是採用類比方 法動態辨別和判斷最佳P I D調試參數的軟體。 經濟部智慧財產局員工消費合作社印製 由於可以僅經由一個約束限制實現速率控制器效果， 因此約束限制的嚴格的控制操作是很重要的。未達最佳標 準的或稍稍保守的調試都可能很容易的導致隨著比合意値 較低的控制操作違反一個約束變數。該操作可能擾亂操作 者或導致操作者啓動速率控制器失敗。 爲了確定優化的調試參數，經由PITOPSTM軟體硏究其 資料並且確定轉移函數。確定五個轉移函數，對應每個 C V - Μ V對，也就是說可控變數和操縱變數對，例如， 約束變數和觸媒進料速率。 在轉移函數確定後，較佳的是進行類比操作，例如， 使用PITOPSTM軟體進行類比。設定通常的給定値變化，典 -53- 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） 523647 Α7 Β7 五、發明説明（5) (請先閲讀背面之注意事項再填寫本頁) 型的無規擾動和白噪音，使得類比儘可能的與真實的控制 行爲接近。然後軟體確定優化的調試參數。此時，進行多 個假定分析在限制範圍內調節觸媒R p Μ的速度產生積極 的和肯定的控制操作。這種類比有助於啓動速率控制方案 前操作者建立信心。 經濟部智慧財產局員工消費合作社印製 在一個複雜製程過程中，例如聚合過程，存在多個操 縱變數可以影響一個單獨的控制變數如生產速率。這些操 縱變數包括，循環反應氣流速，該氣體成分，觸媒生產能 力的改變，反應器壓力等等。這顯示可以有一種多變數設 備，採用任意的市售Μ P C (模型預測控制器）似乎都可 以成爲控制的更合適的設備。但是’ ρ Ε反應器（聚合反 應器的多數特徵）的一個重要特徵是通常只有一個單獨的 關鍵操縱變數可以實現所須的控制變數改變。如此，控制 的問題就變成控制變數和操縱變數的一個稀疏矩陣（對角 矩陣）。換句話說，控制問題不相連的，不象對角矩陣那 樣有一對一的關係。第二特徵是控制變數趨向於成爲不穩 定開環，由於輕微擾動漂移至不穩定螺旋區。該第二特徵 在反應床溫度控制中尤爲明顯。如此，反應控制系統就需 要根據本發明之方法確定控制變數和操作變數中的關鍵動 態關係，並且採用經典的先進的調節控制製程’如ρ 1 D 運算法和串級控制。 給出的實例係關於冷卻限制的具體的約束變數。但是 ，採用的方法可以依照此處的指導擴展至其他的約束變數 ，如所須的生產速率，露點邊界’冷凝物重量百分比，可 -54- 本紙張尺度適用中國國家標準（CNS ) Α4規格（210Χ297公釐） 523647 A7 B7 五、發明説明（θ 冷凝物重量百分比，產物移出（例如，吹掃箱水位），流 化程度，夾帶程度，造粒器、粒狀樹脂傳輸能力和原料添 加（例如進料壓力）。 由於觸媒注入速率的任何改變都會改變反應速率且因 而改變反應熱的產生速率，因此向上和向下調節進入反應 器的循環氣溫度以適應熱生成速率的改變。如此保證了反 應床的溫度不變。完整的使用流化床和循環氣冷卻系統設 備當然有助於監測床層溫度的溫度變化。 在一組給定的工作條件下，經由以粒狀聚合物產品的 形成速率將床的一部分作爲產品移出流化床維持流化床的 恒定高度。因爲反應熱生成速率與產物形成速率直接相關 ，經由反應器的流體的溫度升高値（入口流體和出口流體 的溫差）在恒定流速並且入口流體內沒有可蒸發的流體的 條件下可以指示粒狀聚合物的生成速率。 對於粒狀聚合物產品移出反應器1 0的方法，效果較 佳的是將流體從產品中分出，然後將該流體送回到循環管 2 2。熟悉此藝者有多種方法實現該過程，如JENKINS, III 等人的美爵專利第4，5 4 3，3 9 9號中所述之方法。 流化床反應器能裝上一種充分通風系統（未不出）使 其在啓動和切斷過程中實現流化床通風。反應器不需要使 用攪拌器和/或刮管器。循環管2 2和那裏的部件（壓縮 機3 0，熱交換器2 4 )最好保持其表面平滑，避免不必 要的阻礙使其不至於影響循環氣或霧沬顆粒的流動。 雖然不限於任一特定的反應類型或種類，本發明特別 ---------衣-- (請先閲讀背面之注意事項再填寫本頁) 訂 經濟部智慧財產局員工消費合作社印製 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） -55- 523647 A7 ______ B7 五、發明説明（5¾ 適用於催化裂化和聚合反應，其中包括一種或多種下面列 出的單體之聚合： (請先閲讀背面之注意事項再填寫本頁) 1 .烯烴：例如碳數2 - 2 0，較佳的是2 - 1 5個 碳者，如乙烯、丙烯、1 一 丁烯、1—戊烯、4 一甲基一 1一戊烯、1 一辛烯、1—己烯、苯乙烯。 2 ·極性乙烯單體：如氯乙烯、醋酸乙烯酯、丙烯酸 乙烯酯、甲基丙烯酸甲酯、四氟乙烯、乙烯醚、丙烯腈。 3 ·二烯類（共軛或非共軛者）：如丁二烯、1，4 -己二烯、異戊二烯、亞乙基原冰片烯。 4 .炔烴：如乙炔、取代乙炔、如甲基乙炔。 5 ·醛：如甲醛。 本發明經發現對於烯烴類單體的聚合反應特別有利。 本發明一般可以採用任意種類的觸媒，例如裂化觸媒 和聚合觸媒。例如，上述可在聚合物單體的流化床聚合反 應中採用的觸媒分別包括如下所列： I .配位陰離子觸媒 經濟部智慧財產局員工消費合作社印製 Ϊ I .只用於乙烯共聚反應的陽離子觸媒；其他的同 類的反應需要一種自由基觸媒。 I I I .自由基觸媒或配位陰離子觸媒 IV·配位陰離子觸媒 V ·陰離子觸媒 v I ·茂金屬，如DeCHELLIS等人的美國專利第 5，4 0 5，9 2 2號和CHANG的美國專利第 4 ’ 9 3 7，3 0 1號中所揭示者，以上以引用方式倂於 -56- 本紙張尺度適用中國國家標準（CNS ) A4規格（210X29?公釐） 523647 A7 _B7__ 五、發明説明（5i 本文。 (請先閱讀背面之注意事項再填寫本頁) 在能夠經由本發明之方法生產的聚合物中包括乙烯、 丙烯或丁烯的均聚物或主要摩爾比爲乙烯、丙烯或丁烯而 少數摩爾比爲一種或多種C 2 - C 8 α -烯烴的共聚物 .。該C 2 - C 8 α -烯烴較佳的是在四個碳之間不包含 任何支鏈的煙。較佳的C 2 - C 8 α -烯烴是乙烯、丙 燒、1 一 丁矯、1—戊傭、1 一己傭、4 一甲基一 1 一戊 烯和1 一辛烯。 乙烯均聚物一般密度約爲0 · 958到0 . 972g /cm3，較佳的密度約爲0.958到0·967g/ c m 3，且最佳的密度範圍約爲0 . 9 5 8到0 . 9 6 5 g 經濟部智慧財產局員工消費合作社印製 乙烯共聚物的密度小於Ο _ 9 6 g / c m 3，其範圍約 在 Ο . 890 — Ο · 960g/ cm3，較佳的是 0·910 — 0.958g/cm3，且最佳的是 0 · 910-0 · 955g/cm3。對於一定的共聚物給 定熔融指數的乙嫌共聚物的密度主要是經由改變與乙燃共 聚的C 3 - C 8的共聚用單體的數量來調節的。如果沒有 共聚用單體，乙烯會均聚得到密度約爲〇 . 9 6 g/cm3 的聚合物。如此，加入的共聚用單體的數量越大，共聚物 的密度就下降的越多。在相同的條件下，每種c 3 — c 8 共聚用卓體要得到相问的結果’其需要的數量是不同的。 如此，製備具有相同密度和熔融指數，.大摩爾數的不 同共聚物單體得到的二元共聚物所需的數量順序依次爲 本紙張尺度適用中國國家標準（CNS ) A4規格（210X 297公釐） -57- 523647 A7 _Η_ — 五、發明説明（5¾ C3<C4<C5<C6<C7<C8。 (請先閲讀背面之注意事項再填寫本頁) 當用本處所述的流化床設備生產時，乙烯聚合物是粒 狀的，其體積密度一般爲1 5 - 40 I bm/f t3 ( 24〇-64〇kg/m3)，較佳的是 15 — 38 1 bm /f t3 (240 — 6 l〇kg/m3)，最佳的是 17 — 32 Ibm/f t3 (270-510kg/m3)，其平 均粒徑一般約爲0 . 005 - 0 . 06英尺（〇 . 13 — 1.5mm)，較典型的約爲0 · 010 — 〇 . 〇4〇英 尺（0 . 25 — 1 · 0mm)，最典型的約爲〇. 012 〜0.030 英尺（0· 30 — 0.76mm)，經由篩 網測量。粒徑對於流化流化床反應器的聚合物顆粒是很重 要的。 經濟部智慧財產局員工消費合作社印製 當在冷凝模式工作時，雖然兩相循環氣種的液體含量 可以很高，但是一般要求氣相種夾帶的液相比例一般不超 過約5 0重量％，較佳的是不超過約4 5重量％，最佳的 是不超過約2 0重量％，倘若兩相循環氣的流速足夠高確 保液相夾帶在氣相種並且在反應器中保持流化，其範圍一 般是約2 - 5 0重量％，較佳的是約5 - 4 5重量％，最 佳的是約5 - 4 0重量％。 本發明的時空產率一般不超過3 0 1 b/h r - f t3 (480kg/hr— m3)，一般約爲 5 — 251b/ hr-f t3 (80-400kg/hr-m3)，最典型 的約爲 5 — 20 lb/hr — f t3 (80 — 320kg/ h r - m 3 )。雖然取決於反應器的大小，本發明的生產速 -58- 本紙張尺度適用中國國家標準（CNS ) A4規格（210X 297公釐） 523647 A7 _B7_ ____ 五、發明説明（5¾ (請先閲讀背面之注意事項再填寫本頁) 率〜般約爲1 0 — 1 0 〇噸/小時（9 1 00 一 91 ，000千克/小時），較典型的約爲20 - Θ0噸 /小時（18，000—54，000千克/小時）’最 典型的約30 — 50噸/小時（27，〇〇〇一 4 5，〇 〇 〇千克/小時）。 目標生產速率一般範圍約爲1 〇 一 1 〇 〇噸/小時（ 9070-90，700千克/小時）’較典型的約爲 20 — 60 噸/小時（18，100 - 54，400 千克 /小時），最典型的約爲3 0 - 5 0噸/小時（ 經濟部智慧財產局員工消費合作社印製 27，200 — 45，400千克/小時）。就這點來說 ’決定目標生產速率的因素有庫存量、反應器限制、其他 製程約束限制、有效進料和市場決策。目標冷卻水閥位置 一般爲2 0 % - 1 0 0 %開，較典型的約爲3 0 — 8 0 % 開，最典型的是4 0 - 7 0 %開。目標露點一般不超過 2 0°C，較典型的是不超過1 0°C，最典型的範圍在3 — 7 °C之間。所需的吹掃箱水位一般範圍爲1 0 - 9 5 %， 較典型的是20-80%，最典型的是30-70%。目 標冷凝物重量百分比一般2 - 5 0 %，較典型的約爲5 -45%，最典型的是5-40%。 本發明之方法極大的簡化了聚合反應器控制中的複雜 操作，使其只要調節幾個關鍵約束變數。市售控制器如 Μ P C (模型預測控制）系統被認爲可爲實現該應用的另 一種可能的選擇。但是如前所述，關鍵變數矩陣的稀疏特 性和開環不穩定動態關係使得控制沒有必要使用Μ P C系 -59- 本紙張尺度適用中國國家標準（CNS ) Α4規格（210Χ297公釐） 523647 A7 B7 五、發明説明（ 統。 (請先閲讀背面之注意事項再填寫本頁) 因此，本發明的優點就是反應器的穩定性和控制得到 改善。 因爲反應器的穩定性得到改善’本發明能用於提高生 產。例如，因爲床層溫度的波動減小’溫度可以設定在能 夠優化觸媒活性的區間。就這點來說’一些催化體系對溫 度是很敏感的，如高活性觸媒，如氧化鉻觸媒，齊閣勒-鈉塔觸媒和金屬茂觸媒。 而且，因爲反應器的穩定性得到改善’本發明能提高 產品特性的控制，尤其是對溫度敏感的反應。 改善穩定性的另一個好處就是減少了廢料的產生，減 小環境污染，尤其是對於溫度敏感的反應。 經濟部智慧財產局員工消費合作社印製 本發明還可以經由主動約束最大化生產速率。就這點 來說，本發明連續的調節約束變數參數，如此生產過程得 到準確的控制。在手動操作控制觸媒進料的方法中，操作 者傾向於在一個安全或適宜的區間操作。經由採用本發明 之方法與系統，就不再需要維持上述如此的安全區，操作 者可以安全的維持一個高的平均生產速率。 因此，本發明的另一個優點就是提高了安全性。經由 自動控制觸媒進料，本發明消除了人爲操作失誤的可能性 。除了控制觸媒進料過程中的人爲失誤的可能性外，本發 明還使溫度失控的可能降到最低，例如放熱聚合反應中床 層溫度失控。 本發明的另一個優點在於提高了自動化水平方便了操 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） ~ 523647 A7 __ B7 五、發明説明（5¾ 作者。但是除了經常的調節觸媒進料速率，操作者還可以 注意製程中的其他方面。 (請先閲讀背面之注意事項再填寫本頁) 因此，本發明的控制系統比較於其他控制系統相對的 簡單和經濟。 縱觀上述所有優點，本發明可降低總操作成本。 本發明對於冷卻水△ T ( C W D T )動力學的認識代 表一項重要的發現。 採用本發明的調節控制系統抑制床層溫度波動的協同 作用是本發明的另一重要新穎之處。 雖然，本發明主要係關於反應自動化控制，本發明之 自動控制方面可以與其他反應方面的手動控制相結合。 爲了保持淸晰和簡明，已知的設備在上述的具體描述 中沒有詳細闡述。 本發明要經由以下的實施例進一步闡述。這些實施例 是非限制性實施例，不限制本發明之範圍。 除非特別提及，實施例中所有的百分比、份數等等指 的都是重量比。 經濟部智慧財產局員工消費合作社印製 實施例與比較實施例 以下的具體實施例和比較實施例包括採用Union Carbide公司生產的一種“Unipol G-5000”反應器來聚合乙烯 實施例1 - 3和比較實施例1 本紙張尺ίίϋ中國國家標準（CNS ) A4規格（2丨〇X297公釐） 523647 A7 B7 五、發明説明（5¾ 實施例1 - 3和比較實施例1的具體條件列於表1中 。對於實施例1 — 3 ，控制系統是一種Foxboro IA (T Printed by the Intellectual Property Bureau of the Ministry of Economy ’s Employees ’Cooperatives. The paper size is applicable to the Chinese National Standard (CNS) A4 (210X297 mm) _ 46-523647 Α7 Β7 V. Description of the invention ((Please read the precautions on the back before filling in this (Page) At 408, if the first catalyst feeder is not ready to receive a remote setpoint for some reason (manual, short range, or activated), the preset range will not be downloaded to the rate change mode. Group 2 8 0. Moreover, at 4 1 0, the given 値 will be set to the RP Μ Ρ ID preset given by the current operator. Similarly, if the first catalyst is at 4 1 2 Due to some reasons (manual, short range or start state), the feeder is not ready to receive a given remote command, then the preset command will not be transmitted to the rate change module 2 8 0. Also, at 4 1 4 The given 値 will be set as the RPM PID preset 値 given by the current operator. The logic exits at position 416. The RP shunt logic significantly improves the level of automation and facilitates indoor operation control. When the rate controller When starting, the higher-level controller Based on the given 値 and process conditions, R ρ Μ is generated. The RP 分 shunt logic further divides the total RP 値 値 into the RP 値 required for each block. Because in any case, the total R P M is strictly maintained, so the stability of the control has been significantly improved. Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs, referring again to Figure 7, the given processing logic of the logic controller 2 60 is guaranteed to The stable change of the fixed frame realizes the smooth transition from manual to automatic control. In this regard, if the upstream P IDVALVC 242, WCONC 232, PRATC 212, and P BNLC 2 2 2 are all started by the given frame tracking start, then when these Ρ ID is in the starting state (when the servo RP MP ID is not ready to receive the remote reference), these upstream PP IDs are equal to -47-This paper size applies the Chinese National Standard (CNS) A4 specification (210X297 Mm) 523647 A7 _B7___ 5. Description of the invention (扃 and other corresponding current determinations of 値. This situation is not good because when the control system is started, these ρ 1 〇 The given card needs to be stored and restored (please read the notes on the back before filling out this page). 〇 If the configuration is set to no given card tracking, the given card will be stored according to the last login card, but if the specified card is between the current card and the current card The large rate difference is also unfavorable. The five upstream PID VALVC, PRATC, WCONC, PBNLC, and CWDT must all be set to the given start tracking. Four PID ID VALVC, PRATC, WCONC, and PBNLC must also be set to a given default. Change the rate limit. The disadvantages of the above two examples can be overcome by adding a given unitary processing logic. Figure 10 shows a non-limiting example of a given unitary processing logic. The scan time of the logic block is generally about 1-60 seconds, preferably about 5-30 seconds, and most preferably about 15 seconds. Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs This logic started at 500. At 502, the logic determines whether the cooling water position PID (VALVC) 242 is in manual or automatic state, whether it is in the short range or remote state, and whether it is activated. If the state of V A L V C 2 4 2 is automatic, remote and not activated, then at 504, the reference value of VALVC 242 is set to the maximum allowable value of valve position. If the state of V A L V C is manual or short-range or start, then at 506, the reference of VALVC242 is the current cooling ice valve position. At 508, the logical determination of the weight percentage of condensate (WCONC) -48- This paper size applies the Chinese National Standard (CNS) A4 specification (210X 297 mm) 523647 A7 _B7_ ____ V. Description of the invention (4 (Please read the back first Please pay attention to this page and fill in this page again) Whether 232 is in manual or automatic state, whether WCONC 232 is in short range or remote state, and whether WC NC 2 3 2 is activated. If WCONC 2 3 2 state is automatic, remote and not activated Then, at position 510, the setting of WCONC 232 is set to the maximum allowable condensate. If the state of WC OC NC 2 3 2 is manual or short range or start, then at the position of 5 1 2 'WCONC 2 3 2 Set the current weight percentage of condensate. At 5 1 4, the logic judges whether the production rate PID (PRATC) 212 is in manual or automatic state, whether the Pratc 212 is in the short-range or remote state, and whether the Pratc 2 1 2 is activated. If Pratc 212 status is automatic, remote and not activated, then at 5 1 6 position, the setpoint of PRATC 2 1 2 is set to the required production rate. If the status of PRATC 2 1 2 is manual or short range Start, then at position 518, the given WCONC 232 is the current production rate. The employee consumer cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs prints it at 5 2 0, and the logic determines whether the purge tank water level PID (PBNLC) 222 is in manual or automatic state. , Whether the PBNLC 222 is in the short-range or remote state, and whether the PBNLC 2 2 2 is activated. If the PBNLC 222 state is automatic, remote, and not activated, then at position 522, the PBNLC 222 reference is set to the purge tank water level reference. .If the PBNLC 2 2 2 status is manual or short range or start, then at 524 position, the given value of PBNLC 222 is the current purge box water level. The logic exits at 5 2 6 position. -49- This paper scale applies to China Standard (CNS) A4 specification (210X297 mm) 523647 Α7 Β7 V. Description of the invention (using this logic and standard given 値 tracking design, when the rate control system is started 'all upstream given 値 from their start to the target 値Step. In this way, 'all given frames are stored with their corresponding final frames. At the same time, when the system starts, due to the given frame and actual measurement frame, Large deviations in R ρ in the catalyst feeder caused by large deviations are avoided. Referring to FIG. 7 again, the RPM anti-termination logic controller 2 60 can maintain the automatic control at the catalyst feeder. Within the limits of mechanical properties, such as the maximum catalyst feed rate. The R P M anti-termination logic can protect against system termination when a few blocks are running. For example, if all four blocks are operating at 500 R PM, then the total R PM of the reactor is 2000. If three blocks stall, blocks that run independently will step to the maximum RPM boundary, that is, about 160 ORPM. In this case, the rate controller requires 2 0 0 ORPM, but only 16 0 0 RPM. Then, the loss of production rate is inevitable. In this case, the control logic freezes the internal termination of the upstream PID. Otherwise, the upstream PID will slowly keep increasing its output, and the controller does not know that it cannot reach the rest of the RPM. Figure 11 shows a non-limiting example of the RPM anti-termination logic. The running scan time of the logic block is generally 1 to 60 seconds, preferably 5 to 30 seconds, and most preferably 15 seconds. At 600, logic begins. At 602, 〇 of 〇〇2 is the total RP ′ of the running block and feeder plus 10, which is the tolerance as compared with the low signal selector output 値. At 604, the size of the logical paper is applicable to the Chinese National Standard (CNS) A4 specification (210X297 mm) -5〇 I -------- 衣-(Please read the precautions on the back before filling (This page) Order printed by the Intellectual Property Bureau's Employees' Cooperatives of the Ministry of Economic Affairs 523647 Α7 Β7 V. Invention Description (扃 (Please read the precautions on the back before filling this page) Judge whether R 0 0 2 値 is lower than the low signal selector output 选择2 6 2 small. If R0 0 2 is not less than its output 値 2 6 2, then at 006, B〇〇1 is set to non-true, where RP Μ 値 input to the upstream PID feedback parameter (with Prevent termination) is set equal to the output of the low-signal selector 値 2 6 2 and the logic exits at 6 10. If R〇〇2 is less than its output 値 2 6 2 then at 6 1 2 the logic judges B 0 Whether 0 1 is true. If B〇0 1 is true, the logic exits at 6 1 0. If B〇 01 is not true, β〇〇1 is set to true at 614, and r ρ μ input to the upstream P ID feedback parameter.値 (to prevent termination) is set equal to the output of the low signal selector 値 262, and the logic exits at 610. Because the number 値 1 is added at 6 0 2 This termination protection is activated if the difference between the total R ρ Μ 値 entering the reactor and the output 値 of the low signal selector is greater than 10 R ρ M (tolerance). In general, the low signal selector The output 値 is equal to the total RP Μ 値 entering the reactor, and the mark 〇〇〇1 (internal use only for display purpose) is set to non-true. In this normal state, the feedback 上游 of the upstream P ID is set to be equal to The output of the low signal selector is equal. Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs. When the termination condition is true, the flag 〇〇〇1 is set to true. As long as the condition remains true, the feedback signal is set equal to the last stored low signal The output of the selector 如此. This prevents termination. RPM start logic, RPM shunt logic, given 値 processing logic and RP 终止 anti-termination logic work sequentially or in parallel. It is better to work in parallel, then refer to Figure 7, as shown above The calculation logic of the design is 2-6 0 -51-This paper size applies the Chinese National Standard (CNS) A4 specification (X297 mm) 523647 A7 ——_ B7__ V. Description of the invention (扃 (Please read the (Notes to fill in this page again) The signal 2 7 8 is sent to the rate-change limit block 2 8 0. The rate-change limit block 2 8 0 solves the mechanical limitation of the device that cannot tolerate sudden changes. The rate-change limit block 2 8 0 The signal 2 8 2 is sent to the catalyst RPM controller 290. The RPM controller compares the required speed with the actual speed and adjusts the amperage of the catalyst feeder motor, thereby adjusting the catalyst Feed rate of feeder 16. Figure 12 is a non-limiting example of the operator interface of a production rate controller. There are only three operating items for the operator to choose from: 1 · Enter the required production rate reference. If the rate needs to be maximized, then a high unreachable number should be set, such as 50 tons / hour (907 kg / hour). 2 · Specify the water level of the purge box. In general, there is not much that is necessary to change the given frame. 3 • Activate the rate controller and set one or two feeders to automatic and remote mode. If one feeder is in automatic and remote mode, then the rate controller starts to adjust its R PM setpoint and the other feeder R PM setpoint. Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs To cancel the rate control, both feeders must be set to the short-range mode. Once a suitable setpoint is given, turn the rate controller on, as long as you switch one or both of them from short-range mode to far-end mode, and vice versa. No other operations are required. Figure 13 is a non-limiting example of a separate control display screen provided to the engineer's interface. This display provides more information for checking control performance and ensuring that all aspects of the controller are working well. All detailed specifications of this paper apply Chinese National Standard (CNS) A4 specification (21 × 297 mm) -52- 523647 A7 B7 V. Description of the invention ((Please read the precautions on the back before filling this page) Information is on This screen is given. The display screen allows the operator interface to provide only the information necessary for the operator to keep it simple. Such an arrangement can avoid confusion when training new operators, making all operations and understanding easy and convenient. In a given case, the low-signal selector selects the lowest of the four outputs 値. The selected 重 is highlighted as a box, as shown in Figure 13. At this point, the average and CWDT of the cooling water valve position 位置It is an important indicator to help engineers determine whether the production rate is maximized. It is better to display an average of 20 or 30 minutes. Five PID controllers PRATC, PBNLC, WCONC, CWDTC, VALVC must use one Industrial process control software for accurate debugging. For example, as mentioned above, the PITOPSTM software produced by Artcon, Inc. of Cincinnati, Ohio is dynamically identified by analogy. Software for judging the best PID debugging parameters. Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs. Because the rate controller effect can be achieved through only one constraint limit, the strict control operation of the constraint limit is very important. The optimal standard is not reached. Or slightly conservative debugging may easily cause a constraint variable to be violated with a lower-than-desirable control operation. This operation may disturb the operator or cause the operator to fail to start the rate controller. In order to determine optimized debugging parameters, PITOPSTM software is used to study its data and determine the transfer function. Five transfer functions are determined, corresponding to each CV-MV pair, that is, a pair of controllable and manipulative variables, such as constraint variables and catalyst feed rate. After the transfer function is determined, it is better to perform analog operations, for example, using PITOPSTM software for analogy. To set the usual given changes, Code-53- This paper size applies the Chinese National Standard (CNS) A4 specification (210X297 mm) 523647 Α7 Β7 V. Description of the invention (5) (Please read the notes on the back before filling Page) type of random disturbance and white noise, making the analog as close to the real control behavior as possible. Then the software determines the optimized debugging parameters. At this time, multiple hypothetical analyses are performed to adjust the catalyst R p Μ within the limits. Speed produces positive and affirmative control operations. This analogy helps the operator to build confidence before starting the rate control scheme. The Intellectual Property Bureau of the Ministry of Economic Affairs, employee consumer cooperatives, prints in a complex process, such as the aggregation process. Manipulation variables can affect a single control variable such as production rate. These manipulation variables include the circulating reaction gas flow rate, the gas composition, changes in catalyst production capacity, reactor pressure, and so on. This shows that there can be a multi-variable device, and using any commercially available MPC (model predictive controller) seems to be a more suitable device for control. However, an important feature of the 'ρ Ε reactor (the majority of the characteristics of the polymerization reactor) is that usually there is only a single key manipulated variable to achieve the required control variable change. In this way, the problem of control becomes a sparse matrix (diagonal matrix) of control variables and manipulation variables. In other words, the control problems are not connected and do not have a one-to-one relationship like diagonal matrices. The second characteristic is that the control variable tends to become an unstable open loop, which drifts to the unstable spiral region due to slight disturbances. This second characteristic is particularly evident in the temperature control of the reaction bed. In this way, the reaction control system needs to determine the key dynamic relationship between the control variable and the operation variable according to the method of the present invention, and adopt the classic advanced adjustment control process' such as ρ 1 D algorithm and cascade control. The examples given are specific constraints on cooling limits. However, the method used can be extended to other constraining variables in accordance with the guidance here, such as the required production rate, dew point boundary 'condensate weight percentage, may be -54- This paper size applies Chinese National Standard (CNS) Α4 specifications ( 210 × 297 mm) 523647 A7 B7 V. Description of the invention (θ Condensation weight percentage, product removal (for example, purge tank water level), fluidization degree, entrainment degree, granulator, granular resin transmission capacity and raw material addition (for example Feed pressure). Since any change in the catalyst injection rate will change the reaction rate and thus the reaction heat generation rate, the temperature of the circulating gas entering the reactor is adjusted up and down to accommodate the change in the heat generation rate. This ensures that The temperature of the reaction bed does not change. The complete use of fluidized bed and circulating gas cooling system equipment certainly helps to monitor the temperature change of the bed temperature. Under a given set of working conditions, the formation of granular polymer products The rate removes part of the bed as product from the fluidized bed to maintain a constant height of the fluidized bed. The rate is directly related to the product formation rate. The temperature rise of the fluid passing through the reactor (the temperature difference between the inlet fluid and the outlet fluid) can indicate the rate of formation of granular polymers at a constant flow rate and no vaporizable fluid in the inlet fluid. For the method of removing the granular polymer product from the reactor 10, it is better to separate the fluid from the product, and then return the fluid to the circulation pipe 22. There are many ways to realize the process for those skilled in the art , As described in JENKINS, III, et al., Grand Mercure Patent No. 4,5 4 3, 3 9 9. The fluidized bed reactor can be equipped with a sufficient ventilation system (not shown) to start and Fluidized bed ventilation is achieved during the cut-off process. The reactor does not require the use of agitators and / or scrapers. The circulation tube 22 and the components there (compressor 30, heat exchanger 2 4) preferably keep their surface smooth. To avoid unnecessary obstructions so as not to affect the flow of circulating gas or mist particles. Although not limited to any particular reaction type or kind, the present invention is particularly --------- clothing-(please first Read the notes on the back Fill out this page) Order printed by the Intellectual Property Bureau of the Ministry of Economic Affairs, Consumer Cooperatives. The paper size applies to the Chinese National Standard (CNS) A4 (210X297 mm) -55- 523647 A7 ______ B7 V. Description of the invention (5¾ Applicable to catalytic cracking and Polymerization, including the polymerization of one or more of the monomers listed below: (Please read the notes on the back before filling out this page) 1. Olefins: For example, carbon number 2-2 0, preferably 2-1 5 Individual carbon, such as ethylene, propylene, 1-butene, 1-pentene, 4-methyl-1, 1-pentene, 1-octene, 1-hexene, styrene. 2 · Polar ethylene monomer: such as Vinyl chloride, vinyl acetate, vinyl acrylate, methyl methacrylate, tetrafluoroethylene, vinyl ether, acrylonitrile. 3. Diene (conjugated or non-conjugated): such as butadiene, 1,4-hexadiene, isoprene, ethylidene norbornene. 4. Alkynes: such as acetylene, substituted acetylene, such as methylacetylene. 5 • Aldehydes: such as formaldehyde. The present invention has been found to be particularly advantageous for the polymerization of olefin-based monomers. The present invention can generally use any kind of catalyst, such as cracking catalyst and polymerization catalyst. For example, the above-mentioned catalysts that can be used in the fluidized bed polymerization of polymer monomers include the following: I. Coordinating anionic catalysts Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs I. Only for ethylene Cationic catalyst for copolymerization; other similar reactions require a free radical catalyst. III. Free radical catalyst or coordination anion catalyst IV · coordination anion catalyst V · anion catalyst v I · metallocene, such as US Patent No. 5,040,9 2 2 and CHANG by DeCHELLIS et al. As disclosed in US Patent No. 4 '9 3 7, 3 01, the above is cited by reference to -56- This paper size applies to the Chinese National Standard (CNS) A4 specification (210X29? Mm) 523647 A7 _B7__ 5 Description of the invention (5i this article. (Please read the notes on the back before filling out this page). Polymers that can be produced by the method of the present invention include homopolymers of ethylene, propylene, or butene, or the main molar ratio is ethylene, Copolymer of propylene or butene with a minority molar ratio of one or more C 2 -C 8 α-olefins. The C 2 -C 8 α-olefins preferably do not contain any branching between four carbons Smoke. The preferred C 2 -C 8 α-olefins are ethylene, propylene, 1-butane, 1-pentane, 1-hexane, 4-methyl-1, 1-pentene, and 1-octene. The polymer generally has a density of about 0.9958 to 0.972g / cm3, with a preferred density of about 0.958 to 0.967g / cm3, and the most preferred Density range is about 0.98 to 0.965 g. The density of the ethylene copolymer printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs is less than 〇 _ 9 6 g / cm 3, and the range is about 0. 890 — 〇 · 960g / cm3, preferably 0 · 910 — 0.958g / cm3, and most preferably 0 · 910-0 · 955g / cm3. For a certain copolymer, the density of ethylene copolymers given the melt index is mainly It is adjusted by changing the amount of C 3-C 8 comonomers copolymerized with ethane. If there are no comonomers, ethylene will homopolymerize to obtain a polymer with a density of about 0.96 g / cm 3. In this way, the greater the amount of comonomers added, the more the density of the copolymer decreases. Under the same conditions, each c 3-c 8 copolymer is required to obtain interrogative results. The quantity is different. In this way, the required quantity of binary copolymers obtained from different copolymer monomers with the same density and melt index, and large molar numbers is in order of the paper size in order to apply Chinese National Standard (CNS) A4 specifications (210X 297 mm) -57- 523647 A7 _Η_ — V. Description of the invention (5¾ C3 < C4 < C5 < C6 < C7 < C8. (Please read the notes on the back before filling out this page). When produced with fluidized bed equipment as described here, the ethylene polymer is granular. Bulk density is generally 15-40 I bm / f t3 (240-64 kg / m3), preferably 15-38 1 bm / f t3 (240-6 lkg / m3), the best It is 17 — 32 Ibm / f t3 (270-510kg / m3), and its average particle size is generally about 0.005 to 0.06 feet (0.13 to 1.5mm), more typically about 0. 010 to 〇 .04 feet (0. 25 — 1.0 mm), most typically about .012 to 0.030 feet (0. 30 — 0.76 mm), measured through a screen. Particle size is important for polymer particles in a fluidized bed reactor. Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs. When working in condensing mode, although the liquid content of the two-phase circulating gas species can be very high, it is generally required that the proportion of liquid phase entrained by the gas phase species does not exceed about 50% by weight It is preferably not more than about 45% by weight, and most preferably not more than about 20% by weight. If the flow rate of the two-phase circulating gas is sufficiently high to ensure that the liquid phase is entrained in the gas phase and remains fluidized in the reactor, The range is generally about 2 to 50% by weight, preferably about 5 to 45% by weight, and most preferably about 5 to 40% by weight. The space-time yield of the present invention generally does not exceed 3 0 1 b / hr-f t3 (480kg / hr-m3), generally about 5-251b / hr-f t3 (80-400kg / hr-m3), the most typical Approximately 5-20 lb / hr-f t3 (80-320kg / hr-m 3). Although it depends on the size of the reactor, the production speed of the present invention is -58- This paper size is applicable to the Chinese National Standard (CNS) A4 specification (210X 297 mm) 523647 A7 _B7_ ____ 5. Description of the invention (5¾ (Please read the Note for refilling this page) The rate is usually about 10-100 tons / hour (9 1 00-91,000 kg / hour), more typically about 20-Θ0 tons / hour (18,000- 54,000 kg / hour) 'The most typical is about 30-50 tons / hour (27,400-55,000 kg / hour). The target production rate generally ranges from about 10,000 tons / Hour (9070-90,700kg / hour) 'more typical is about 20-60 tons / hour (18,100-54,400kg / hour), the most typical is about 30-50 tons / hour (Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs at 27,200 — 45,400 kg / hour.) In this regard, the factors that determine the target production rate are inventory, reactor constraints, other process constraints, and effective progress. Material and market decisions. Target cooling water valve position is generally 20%-100% open , The most typical is about 30-80% open, the most typical is 40-70% open. The target dew point generally does not exceed 20 ° C, the more typical is not more than 10 ° C, the most typical The range is between 3-7 ° C. The required purge tank water level is generally in the range of 10-95%, more typically 20-80% and most typically 30-70%. Target condensate weight percentage Generally 2-50%, more typically about 5-45%, and most typically 5-40%. The method of the present invention greatly simplifies the complicated operation in the control of the polymerization reactor, so that it only needs to adjust a few key Constrained variables. Commercially available controllers such as M PC (Model Predictive Control) systems are considered to be another possible option for this application. But as mentioned earlier, the sparse nature of the key variable matrix and the open-loop unstable dynamic relationship It makes it unnecessary to use Μ PC series-59- This paper size is applicable to Chinese National Standard (CNS) A4 specification (210 × 297 mm) 523647 A7 B7 V. Description of invention (system. (Please read the precautions on the back before filling this page ) Therefore, the advantage of the present invention is that the stability and control of the reactor are improved Because the stability of the reactor is improved, the present invention can be used to increase production. For example, because fluctuations in bed temperature are reduced, the temperature can be set to a range that can optimize catalyst activity. In this regard, some catalytic systems It is very sensitive to temperature, such as highly active catalysts, such as chromium oxide catalysts, Ziegler-Sodium catalysts and metallocene catalysts. Moreover, since the stability of the reactor is improved ', the present invention can improve the control of product characteristics, especially the temperature-sensitive reaction. Another benefit of improved stability is reduced waste generation and reduced environmental pollution, especially for temperature-sensitive reactions. Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs The present invention can also maximize the production rate through active restraint. In this regard, the present invention continuously adjusts the constraint variable parameters so that the production process is accurately controlled. In the method of manually controlling the catalyst feed, the operator tends to operate in a safe or suitable interval. By adopting the method and system of the present invention, it is no longer necessary to maintain such a safe area, and the operator can safely maintain a high average production rate. Therefore, another advantage of the present invention is improved security. By automatically controlling the catalyst feed, the present invention eliminates the possibility of human error. In addition to controlling the possibility of human error in the catalyst feed process, the invention also minimizes the possibility of temperature runaway, such as runaway bed temperature during exothermic polymerization. Another advantage of the present invention is that it improves the level of automation and facilitates the operation of the paper. The paper size is applicable to the Chinese National Standard (CNS) A4 specification (210X297 mm) ~ 523647 A7 __ B7 V. Description of the invention (5¾ author. But in addition to the regular adjustment touch Media feed rate, the operator can also pay attention to other aspects of the process. (Please read the precautions on the back before filling out this page) Therefore, the control system of the present invention is relatively simple and economical compared to other control systems. With all the advantages, the present invention can reduce the total operating cost. The understanding of the cooling water △ T (CWDT) dynamics of the present invention represents an important discovery. The synergistic effect of using the regulating control system of the present invention to suppress the temperature fluctuation of the bed is the present invention Another important novelty. Although the present invention is mainly related to reaction automation control, the automatic control aspect of the present invention can be combined with the manual control of other reaction aspects. In order to maintain clarity and conciseness, the known equipment is described above It is not described in detail in the detailed description. The present invention is further explained by the following examples. These examples are non-limiting examples and do not limit the scope of the present invention. Unless specifically mentioned, all percentages, parts, etc. in the examples refer to weight ratios. Printed by the Consumer Cooperative of Intellectual Property Bureau of the Ministry of Economic Affairs Examples and Comparative Examples The following specific examples and comparative examples include the use of a "Unipol G-5000" reactor produced by Union Carbide to polymerize ethylene. Examples 1-3 and Comparative Example 1 This paper ruler Standard (CNS) A4 specification (2 ×× 297 mm) 523647 A7 B7 V. Description of the invention (5¾ The specific conditions of Examples 1-3 and Comparative Example 1 are listed in Table 1. For Examples 1-3, the control The system is a Foxboro IA (
Intelligent Automation)控制系統，其程式邏輯列於第7 圖- 1 1。在比較實施例1中，觸媒進料速率是手動控制 .的。 在表1中，“承載T i ”指的是四氫呋喃、氯化鎂、 氯化鈦經氯化二乙基鋁（二氯化乙基鋁對四氫呋喃的比例 是0 . 5 )和三乙基鋁（三乙基鋁對四氫呋喃的比例是 0 . 2 5 )還原的複合物，浸沒在三乙基鋁處理的二氧化 矽中。“鉻（1 ) ”指的是二氧化矽承載的氧化鉻觸媒。 “鉻（2 ) ”指的是一種二氧化砂承載的鉻酸二—（三苯 基）砂院基酯，包含0 . 2 5重量％的鉻。 (請先閱讀背面之注意事項再填寫本頁) 經濟部智慧財產局員工消費合作社印製 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） -62- 523647 A7 B7 五、發明説明（6¾ 表1 經濟部智慧財產局員工消費合作社印製 特性質： 實施例 1 實施例 2 實施例 3 比較實 施例1 循環乙烯 (bar(kg/cm2)) 9(9) 9(9) 14(14) 14(14) 循環H2/C2(摩爾比） 0.14 0.14 0.02 0.02 循環C6/C2(摩爾比） 0.14 0.14 0.01 0.005 循環 N2(bar(kg/cm2)) 10(10) 10(10) 5(5) 5(5) 循環氣流露點（乾燥 模式）（°C ) 32 38 循環異戊烷（bar) 0.3 0.3 1.5 1.3 循環氣流中的冷凝 物重量％(冷凝模式） 6 8 觸媒 承載Ti 承載Ti 鉻⑴ 鉻（2) 活化劑組成 三甲 基絕 三甲 基鋁 無 紐 反應器溫度（°C ) 86 86 1 05 95 反應器壓力（bar) 21 21 21 21 流化床表面氣速 (m/s) 0.72 0.72 0.72 0.72 時空產率 (lb/hr/ft3(kg/hr/m3)) 11(180) 11(180) 10(160) 7.6(120) (請先閲讀背面之注意事項再填寫本頁) 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） 523647 A7 B7 五、發明説明（6) 實施例1 (請先閱讀背面之注意事項再填寫本頁) 在此實施例中，生產速率控制器將反應器速率與冷卻 水約束變數始終維持接近的能力表示出來。生產速率輕微 變化，總是保證維持冷卻水約束變數（c W D T給定値） 〇 第1 4圖示出的是生產速率能夠經由調節觸媒進料速 率和最小化冷卻水△ T，達到生產速率的最大化。在第 1 4圖中，生產速率的單位是t 〇 n/h r ，吹掃箱水位 的單位是米，冷凝物的重量比是百分比，冷卻水閥位置是 百分比開度，冷卻水△ T的單位是°C。C W D T給定値是 1°C，生產速率給定値是32 t on/hr。 實施例2 經濟部智慧財產局員工消費合作社印製 第1 5圖中，生產速率控制器從一個約束變數轉移到 另一個約束變數，藉此連續的優化反應速率的能力得到了 表示。在第1 5圖中，生產速率的單位是t 〇 n/h r ， 吹掃箱水位的單位是米，冷凝物的重量比是百分比，冷卻 水閥位置是百分比開度，冷卻水△ T的單位是°C。生產速 率的初始給定値是1 9 t ο n / h I*，其最終給定値是 40 t on/hr。CWDT 給定値是 1°C。 參照第1 5圖，反應器在開始時有一個下行約束變數 (由於粒狀樹脂的處理和混合），這就需要生產速率維持 一個較低値。爲了緩解這種約束變數，經由調節生產速率 控制器的給定値自動的提高反應速率，直至達到第二約束 -64- 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） 523647 A7 B7_ 五、發明説明（6$ 變數，如此優化了反應速率。 (請先閱讀背面之注意事項再填寫本頁) 實施例3 此實施例闡明經由一種閉環觸媒進料控制器調節進料 速率改善系統的穩定性。就這點來說，維持反應器內的觸 媒量是很重要的。第1 6圖表示生產速率的變化與反應器 中觸媒的量直接相關。觸媒的生產力不變的情況下，在反 應器內維持穩定的觸媒量對於維持高的平均生產速率是重 要的。 在第16圖中，生產速率的單位是ton/hr ，吹 掃箱水位的單位是米，冷凝物的重量比是百分比，冷卻水 閥位置是百分比開度，冷卻水△ T的單位是°C。生產速率 的初始給定値是3 2 t ο n / h r ，其最終給定値是3 2 t on/hr。CWDT 給定値是 1 1 · 5它。 比較實施例1 經濟部智慧財產局員工消費合作社印製 此比較實施例顯示了露點控制函數在防止板淤塞造成 的反應器中斷中的重要性。第1 7圖表示了露點在兩天內 的變化，向下漂移。 低的露點導致了分散板（分散器板）迅速淤塞，引起 壓降的上升。該壓降導致了反應器中斷。經由本發明的連 續調節露點和控制反應以保證操作接近冷凝時不進入低露 點區，避免反應器中斷。 -65- 本紙張尺度適用中國國家標準（CNS ) A4規格（210 X 297公釐） 523647 A7 B7 五、發明説明（6¾ 實施例4 一 6和比較實施例2 - 4 (請先閲讀背面之注意事項再填寫本頁} 實施例4和比較實施例2的反應條件和實施例3相同 ，如表1所示。在實施例5和比較實施例3中，反應條件 和比較實施例1相同，如表1所示。在實施例6和比較實 施例4中，反應條件和實施例1和2相同，如表1所示。 在這些實施例中，控制系統和實施例1中相同。在比 較實施例中，觸媒進料速率時手動控制的。 表2總結了在接近約束速率條件下，幾天的操作後的 生產速率。 表2 在市售反應器中證實的生產速率改良（對天數進行平均） -----—-- ----— 實施例 觸媒 CWDT最小値 (°c ) —---— 生產速率 (標準化） 4 鉻⑴ 11.5 1 06 5 鉻（2) 8.9 ---- 1 08 6 承載Ti 2.5 ----- 1 05 比較實施例2 鉻⑴ 14.9 ---—^_ 1 00 比較實施例3 鉻(2) 12.6 ------ 1 00 比較實施例4 承載Ti 3.5 1 00 經濟部智慧財產局員工消費合作社印製 如此，顯示了生產速率至少有5 %的增量。 實i例7 — ft和比齩實施例5 — 6 以下的實施例和比較實施例顯示了基於C W D T的控 尺 I張 -紙 本 適 準 標 家 國 i國 -66- 523647 A7 B7 五、發明説明（ (請先閲讀背面之注意事項再填寫本頁) 制對整個生產速率最大化的重要優點，該控制是經由嚴格 執行冷卻水真實邊界來實現的。第二個優點就是串級控制 系統有效的抑制了床層溫度飄移。c W D T控制器作用保 證了當接近C W D T限制時，減小觸媒的R P Μ値，床層 溫度不會一直偏離給定値。如果一個觸媒提取區塊下降， CWDT控制器還會自動的提升觸媒RPM，以保持維持 C W D Τ 値。 在實施例7和比較實施例5中，反應條件和實施例1 相同，列於表1中。實施例8和比較實施例6 ，反應條件 和實施例1和2相同，列於表1中。 在這些實施例中，控制方案和實施例1相同。比較實 施例中，觸媒進料速率是手動控制的。 以下的資料顯示生產速率得到明顯的提高，尤其對於 鉻（1 )觸媒’主要是由於生產速率控制以及其與溫度的 協合效應。 表3 經濟部智慧財產局員工消費合作社印製 使用速率控制器和不使用速率控制器時床層溫度的標準偏 差 實施例 床層溫度標準偏差（°C ) 評價 7 0.34 明顯改善 8 0.24 比較實施例5 0.63 比較實施例6 0.22 -67- 本紙張尺度適用中國國豕標準（CNS ) Α4規格（21〇 X 297公釐） 523647 Α7 Β7 五、發明説明（6¾ (請先閲讀背面之注意事項再填寫本頁) 雖然本發明是經由和一些特定的較佳的實施例聯繫進 行描述的’因此這些實施例方面的內容可以被很好的理解 ’但本發明並不局限於這些特定的例子。相反，本發明應 該包括所有的替代的，修改的和相當的方法，包含在後面 附帶的發明申請範圍中。 範例搾制系統命名法附錄 B I 〇 η代表了輸入到控制邏輯模組的一個二進位輸 入値。Β ◦ 〇 η代表由控制邏輯模組產生的二進位輸出値 。I I Ο η代表了輸入到控制邏輯模組的整數輸入値。 I〇Ο η代表了由控制邏輯模組產生的一個整數輸出信號 。R I Ο η代表了輸入到控制邏輯模組的一個實數（浮點 )輸入信號。R〇Ο η代表了控制邏輯模組產生的一個實 數輸出信號。Μ n m代表了 一個內部變數，其値在控制邏 輯模組連續的執行過程中需要存儲。“〜”代表負號。〜 (真）二非真。〜（非真）=真。 經濟部智慧財產局員工消費合作社印製 R P Μ啓動玀鼯 實數輸入値:RI 0 1=進料器# 1現時RPM値； RI02=進料器#2現時RPM値。 ~~>進位輸入値•·ΒΙ01==進料益#1 RPM Ρ I D的手動/自動狀態（手動=0，自動=1 ); Β I 0 2 =進料器# 1 R Ρ Μ Ρ I D的近程/遠端狀 態（近程=0，遠端=1) ;ΒΙ03=進料器#1 -68- 本紙張尺度適用中國國家標準（CNS ) Α4規格（21〇><297公釐） 經濟部智慧財產局員工消費合作社印製 523647 A7 B7_ 五、發明説明（6¾ R Ρ Μ P ID的啓動狀態（啓動=1’未啓動=〇); BI〇4=進料器#2 RPM PID的手動/自動狀 態（手動=〇，自動=]_) ;BI05=進料器#2 R Ρ Μ ρ I D的近程/遠端狀態（近程=〇，遠端=1 );Β I 0 6 =進料器# 2 R Ρ Μ Ρ I D的啓動狀態 (啓動=1，未啓動=0) ;ΒΙ07=進料器1#區塊 # 1狀態（0 =關，1 =開）；Β 1 〇 8 =進料器# 1區 塊# 2狀態（0 =關，1 =開）；Β 1 〇 9 =進料器# 1 馬達狀態（0 =停止，1 =運行）；Β 1 1 〇 =進料器 # 2區塊# 1狀態（〇 =關，1二開）；Β I 1 1 =進料 器#2區塊#2狀態（0二關，1=開）；Β I 12=進 料器# 2馬達狀態（0 =停止，1 =運行） 實數輸出:RO 〇 1 =當速率控制器關時，啓動上游 Ρ I D (啓動參數）的總的R Ρ Μ値；R〇〇 2 =當速率 控制器打開，僅做演示目的的上游Ρ I D啓動總的R Ρ Μ 値。 整數輸出:1〇〇1=進料器#1中向反應器中添加 料的區塊的數目；1〇〇2二進料器#2中向反應器中添 加料的區塊的數目；I〇〇 3 =向反應器中添加的總的 R Ρ Μ 値。 二進位輸出:如果Β〇0 1二0顯示進料器# 1沒準 備好接收遠端給定値；如“ =1 ”顯示進料器# 1準備接 收遠端給定値；如果Β〇0 2 = 0顯示進料器# 2未準備 好接收遠端給定値；如“二1 ”顯示進料器# 2準備接收 本紙張尺度適用中國國家標準（CNS ) Α4規格（210X297公釐） _ ~ " (請先閲讀背面之注意事項再填寫本頁)Intelligent Automation) control system, its program logic is listed in Figure 7-1 1. In Comparative Example 1, the catalyst feed rate was manually controlled. In Table 1, "supporting Ti" refers to tetrahydrofuran, magnesium chloride, titanium chloride via diethylaluminum chloride (ratio of ethylaluminum dichloride to tetrahydrofuran is 0.5) and triethylaluminum (three The ratio of ethylaluminum to tetrahydrofuran is 0.25) The reduced complex is immersed in triethylaluminum-treated silicon dioxide. "Chromium (1)" refers to a chromium oxide catalyst supported by silicon dioxide. "Chromium (2)" refers to a di- (triphenyl) sulphonyl ester of chromic acid supported on sand dioxide, containing 0.25% by weight of chromium. (Please read the precautions on the back before filling this page) The paper size printed by the Employees' Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs applies to the Chinese National Standard (CNS) A4 specification (210X297 mm) -62- 523647 A7 B7 V. Description of the invention (6¾ Table 1 Printed properties of employee cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs: Example 1 Example 2 Example 3 Comparative Example 1 Recycled ethylene (bar (kg / cm2)) 9 (9) 9 (9) 14 ( 14) 14 (14) Cycle H2 / C2 (molar ratio) 0.14 0.14 0.02 0.02 Cycle C6 / C2 (molar ratio) 0.14 0.14 0.01 0.005 Cycle N2 (bar (kg / cm2)) 10 (10) 10 (10) 5 ( 5) 5 (5) Dew point of circulating air flow (dry mode) (° C) 32 38 circulating isopentane (bar) 0.3 0.3 1.5 1.3 wt% of condensate in circulating air flow (condensing mode) 6 8 Catalyst carrying Ti carrying Ti Chromium ⑴ Chromium (2) Activator composition Trimethylaluminum trimethylaluminum reactor temperature (° C) 86 86 1 05 95 Reactor pressure (bar) 21 21 21 21 Gas velocity on the surface of the fluidized bed (m / s) 0.72 0.72 0.72 0.72 Space-time yield (lb / hr / ft3 (kg / hr / m3)) 11 (180) 11 (180) 10 (160) 7.6 (120) (Please read the back first Please note this page before filling in this page) This paper size applies the Chinese National Standard (CNS) A4 specification (210X297 mm) 523647 A7 B7 V. Description of the invention (6) Example 1 (Please read the precautions on the back before filling this page ) In this embodiment, the production rate controller expresses the ability of the reactor rate and the cooling water constraint variable to always remain close. The production rate is slightly changed, always ensuring that the cooling water constraint variable is maintained (c WDT given 値) 〇 1 Figure 4 shows that the production rate can be maximized by adjusting the catalyst feed rate and minimizing the cooling water ΔT. In Figure 14, the unit of the production rate is t 0 n / hr. The unit of the water level of the sweep box is meters, the weight ratio of the condensate is a percentage, the position of the cooling water valve is a percentage opening, and the unit of the cooling water △ T is ° C. The CWDT setting is 1 ° C and the production rate is 32 t. on / hr Example 2 Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs Figure 15. The production rate controller is transferred from one constraint variable to another constraint variable, thereby continuously optimizing Ability reaction rate was expressed. In Figure 15, the unit of the production rate is t 〇n / hr, the unit of the purge tank water level is meters, the weight ratio of the condensate is a percentage, the position of the cooling water valve is a percentage opening, and the unit of cooling water △ T Is ° C. The initial setpoint for the production rate is 19 t ο n / h I *, and the final setpoint is 40 t on / hr. The CWDT reference is 1 ° C. Referring to Figure 15, the reactor has a downward constraining variable at the beginning (due to the handling and mixing of the granular resin), which requires a low production rate to be maintained. In order to alleviate this constraint variable, the response rate is automatically increased by a given value of the production rate controller until the second constraint is reached -64- This paper size applies the Chinese National Standard (CNS) A4 specification (210X297 mm) 523647 A7 B7_ V. Description of the invention (6 $ variable, which optimizes the reaction rate. (Please read the notes on the back before filling this page) Example 3 This example illustrates the adjustment of the feed rate improvement system through a closed-loop catalyst feed controller In this regard, it is important to maintain the amount of catalyst in the reactor. Figure 16 shows that the change in production rate is directly related to the amount of catalyst in the reactor. The productivity of the catalyst is unchanged In the case, maintaining a stable amount of catalyst in the reactor is important to maintain a high average production rate. In Figure 16, the unit of the production rate is ton / hr, the unit of the water level of the purge tank is meters, and the condensate The weight ratio is percentage, the position of the cooling water valve is the percentage opening, and the unit of cooling water △ T is ° C. The initial setting of the production rate is 3 2 t ο n / hr, and the final setting is Yes 3 2 t on / hr. The given CWDT is 1 1 · 5 it. Comparative Example 1 Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs This comparative example shows that the dew point control function prevents reactor interruption caused by board fouling Figure 17 shows the change in dew point over two days, drifting downwards. The low dew point causes rapid dispersal of the dispersion plate (dispersor plate), causing an increase in pressure drop. This pressure drop leads to a reaction The device is interrupted. The continuous adjustment of the dew point and the control reaction of the present invention ensure that the operation does not enter the low dew point area when the operation is close to condensation, so as to avoid reactor interruption. -65- This paper size is applicable to the Chinese National Standard (CNS) A4 specification (210 X 297) (%) 523647 A7 B7 V. Description of the invention (6¾ Example 4-1 and Comparative Examples 2-4 (Please read the notes on the back before filling out this page} Reaction conditions and examples of Example 4 and Comparative Example 2 3 is the same as shown in Table 1. In Example 5 and Comparative Example 3, the reaction conditions are the same as in Comparative Example 1, as shown in Table 1. In Example 6 and Comparative Example 4, the reaction conditions and implementation are example 1 and 2 are the same, as shown in Table 1. In these examples, the control system is the same as in Example 1. In the comparative example, the catalyst feed rate was manually controlled. Table 2 summarizes the near-constrained rate Production rate after several days of operation under conditions. Table 2 Production rate improvement confirmed in commercially available reactors (average of days) --------------------- Example catalyst minimum CWDT値 (° c) —---— Production rate (standardized) 4 Cr ⑴ 11.5 1 06 5 Chromium (2) 8.9 ---- 1 08 6 Carrying Ti 2.5 ----- 1 05 Comparative Example 2 Cr ⑴ 14.9 ----- ^ _ 1 00 Comparative Example 3 Chromium (2) 12.6 ------ 1 00 Comparative Example 4 Carrying Ti 3.5 1 00 Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs, showing production The rate must be increased by at least 5%. Example 7-ft and ratio Example 5-6 The following examples and comparative examples show a CWDT-based ruler sheet-a paper standard, a standard country-66- 523647 A7 B7 V. Invention Explanation (Please read the notes on the back before filling this page) The important advantage of maximizing the entire production rate is that the control is implemented by strictly implementing the true boundary of the cooling water. The second advantage is that the cascade control system is effective The temperature of the bed is suppressed. C The WDT controller function ensures that when the CWDT limit is approached, the catalyst's RP M is reduced, and the bed temperature does not always deviate from the given temperature. If a catalyst extraction block drops, CWDT The controller will also automatically raise the catalyst RPM to maintain the CWD T. In Example 7 and Comparative Example 5, the reaction conditions are the same as in Example 1, and are listed in Table 1. Example 8 and Comparative Example 6. The reaction conditions are the same as in Examples 1 and 2, and are listed in Table 1. In these examples, the control scheme is the same as in Example 1. In the comparative examples, the catalyst feed rate was manually controlled. The following information It shows that the production rate has been significantly improved, especially for the chromium (1) catalyst, which is mainly due to the production rate control and its synergistic effect with temperature. Standard deviation of bed temperature when using a rate controller Example Bed temperature standard deviation (° C) Evaluation 7 0.34 Significant improvement 8 0.24 Comparative example 5 0.63 Comparative example 6 0.22 -67- This paper scale applies Chinese national standard (CNS) A4 specification (21 × X 297 mm) 523647 Α7 B7 V. Description of the invention (6¾ (Please read the notes on the back before filling this page) Although the present invention is related to some specific preferred embodiments The description "therefore, the content of these embodiments can be well understood", but the present invention is not limited to these specific examples. Instead, the present invention should include all alternatives, modifications and equivalent methods, including In the scope of the invention application attached below, Appendix BI of the example press system nomenclature represents the input to the control logic module. A binary input 値. B ◦ η represents the binary output 値 generated by the control logic module. II 〇 η represents the integer input 输入 input to the control logic module. I 〇 η represents the control logic module An integer output signal generated. RI ο η represents a real (floating point) input signal input to the control logic module. R 〇 η represents a real output signal generated by the control logic module. Μ nm represents a Internal variables whose values need to be stored during the continuous execution of the control logic module. "~" Stands for negative sign. ~ (True) Second is not true. ~ (Not true) = true. Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs. R PM Started. Real number input: RI 0 1 = Feeder # 1 current RPM 値; RI02 = Feeder # 2 current RPM 値. ~~ & Carry input 値 • · ΒΙ01 == Manual / Automatic status of feed material # 1 RPM Ρ ID (manual = 0, automatic = 1); Β I 0 2 = Feeder # 1 R Ρ Μ Ρ ID Proximity / remote state (proximity = 0, distal = 1); ΒΙ03 = Feeder # 1 -68- This paper size applies the Chinese National Standard (CNS) Α4 specification (21〇 > < 297) (B) Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs 523647 A7 B7_ V. Description of the invention (6¾ R Ρ Μ P ID activated state (activated = 1'not activated = 〇); BI〇4 = Feeder # 2 RPM Manual / automatic status of PID (manual = 〇, automatic =] _); BI05 = proximity / distance status of feeder # 2 R Ρ Μ ρ ID (proximity = 0, remote = 1); Β I 0 6 = Initiator status of Feeder # 2 R Ρ Μ Ρ ID (Startup = 1, Not Started = 0); ΒΙ07 = State of Feeder 1 # Block # 1 (0 = Off, 1 = On); B 1 〇8 = state of feeder # 1 block # 2 (0 = off, 1 = on); B 1 〇9 = state of feeder # 1 (0 = stopped, 1 = running); B 1 1 〇 = State of feeder # 2 block # 1 (0 = off, 1 on); β I 1 1 = state of block # 2 of feeder # 2 (0 off, 1 = on); I 12 = Feeder # 2 Motor status (0 = Stop, 1 = Run) Real output: RO 〇1 = When the rate controller is off, start the total R ρ Μ 値 of the upstream P ID (start parameter); R 〇〇2 = When the rate controller is turned on, only the upstream P ID used for demonstration purposes starts the total R P Μ 値. Integer output: 1001 = The block in Feeder # 1 that adds material to the reactor Number; the number of blocks added to the reactor in the 002 binary feeder # 2; IO03 = the total RP Μ 値 added to the reactor. Binary output: if B〇 0 1 2 0 shows that feeder # 1 is not ready to receive the remote setpoint; for example, “= 1” shows that feeder # 1 is ready to receive the remote setpoint; if 〇〇 2 2 = 0 displays feeder # 2 Not ready to receive the remote reference; such as "two 1" shows feeder # 2 is ready to receive This paper size applies Chinese National Standard (CNS) Α4 specification (210X297 mm) _ ~ " (Please read the note on the back first (Fill in this page again)
523647 A7 B7 五、發明説明（ 遠端給定値；B 0 0 3 = “ 〇，，表示“啓動” *能運行高 級控制程式’ 1 '顯示至少一個襲可以接受給定値， 高級控制程式準備運行。B〇〇 4 = — B ◦ (；) 3 經濟部智慧財產局員工消費合作社印製 R P Μ 分流邏輯_ 實關A_: R 1 0 1 =低信號選擇器的輸出値 圖所不LOSEL) ;Ri〇2=現時的進料器# 疋値，R I 0 3二現時的# 2進料器的r ρ μ給定値 一氣位皁命Λ, : Β 1 〇 1 = D c S控制邏輯模組的 Β〇〇 1 (如“ 0顯示進料器# i未準備接受遠 値。如“ 1 ”顯示進料器#丨準備接受遠端給定値。 B I 〇 2等=D C S控制邏輯模組的b〇〇 2 (如 顯示進料器# 2未準備接受遠端給定値。如“ 1 ” 料器#2準備接受遠端給定値。）bI〇3=DC 邏輯模組的B〇0 3 ( “ 〇 ”表示“啓動”，無法 級控制程式。“ 1 ”表示至少一個模組可以接受遠 値，可以打開高級控制程式。） 整數輸入:I I 〇 1 = D C S控制邏輯模組I (觸媒進料器# 1的進料區塊數目）；I I 0 2 = 控制邏輯模組I ◦ 0 2 (觸媒進料器# 2的進料區 (第6 1的給 端給定 )“ 0，， 顯示進 s控制 轉入高 端給定 〇 0 1 DCS 塊數目 實數輸出:R〇0 1 =自動遠端模式下的RPM値（ 可以經由速率控制器調節的R P Μ -可以下傳遠端給定® );R〇〇 2 =手動和近程模式下的R P Μ値（不可以經 本紙張尺度適用中國國家標準（CNS ) Α4規格（21〇><297公釐） -70 - {請先閲讀背面之注意事項再填寫本頁} 523647 A7 --------B7____ 五、發明説明（d 由速率控制器調節的R P Μ -不可以下傳遠端給定値）； R〇0 3 =進料器# 1速率變換模組的R Ρ Μ給定値； (請先閲讀背面之注意事項再填寫本頁) R〇0 4二進料器# 2速率變換模組的R Ρ Μ給定値。 整數變數:Μ0 1=進料器# 1 RPM處於操作者 控制下（R Ρ Μ Ρ I D處於手動或近程模式）；Μ 0 2 =進料器# 1 RPM處於操作者控制下（RPM Ρ I D處於手動或近程模式） 値處理邏鍇 1數輸入:R I 0 1 =CW閥最大允許邊界値； R I 0 2=冷凝物重量百分比最大允許値；R I 0 3=現 時的CW閥位置；R I 0 4=現時的冷凝物重量百分比； R 1 〇 5 =合意的生產速率給定値；R I〇6現時的生產 速率；R I 〇 7 =吹掃箱水位給定値；r I 〇 8二現時的 吹掃箱水位給定値 經濟部智慧財產局員工消費合作社印製 二進位輸入:B I 〇 1二CW閥位置Ρ I D標記名 VALV C的手動/自動模式（手動=〇，自動=1 ); B I 02=VALVC的近程/遠端（自動/PCAS) 模式；B I 〇 3 = V A L V C的啓動狀態（跟蹤）（啓動 一1 ’未啓動=〇);BI04=冷凝物重量百分比 p I D標記名WCONC的手動/自動模式（手動=0， 自動=1) ;6 1〇5=界（：〇^(：的近程/遠端（自動 / P C A S )模式；B I 〇 6 = W C〇N C的啓動狀態（ 跟蹤）（啓動=1，未啓動=〇) ;BI〇7=速率控制 -71 - 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） 523647 Α7 _ Β7 五、發明説明（6¾ (請先閲讀背面之注意事項再填寫本頁) ΡID標記名PRATC的手動/自動模式（手動二〇 自動=1) ;BI〇8 = PRATC的近程//遠端（自動 /PCAS)模式；Β I 〇9 = PRatc的啓動狀態（ 跟蹤）（啓動=1 ，未啓動二0 ) ; Β I丨〇 =吹掃箱水 位 Ρ I D標記名P BNL C的手動/自動模式（手動= 0，自動=1) ;biii = pbnlc的近程/遠端（ 自動/PCAS)模式；ΒI〇9=PBNLC的啓動狀 態（跟蹤）（啓動=1，未啓動=〇 )。 實數輸出:R〇0 1 ^CW閥位置p I d標記名 VALV C給定値；R〇〇 2 =冷凝物重量百分比ρ I d 標g己名W C〇N C給定値；R〇〇 3 =速率控制ρ I D標 g己名P R A T C給定値；R〇〇 4 =吹掃箱水位ρ I D標 記名P B N L C給定値。 M 防終止 玀輾 實數„皇入:R I 0 1 =進料器# 1的現時的rpm給 定値；R I 0 2 =進料器# 2的現時的R p Μ給定値； 經濟部智慧財產局員工消費合作社印製 R I 0 3=低信號選擇器標記名LOSEL的輸出値（見 第7圖）。 整1輸入:I I 〇 1 =控制邏輯模組I 0 0 1 (觸媒 進料器# 1的進料區塊數目）；I I 〇 2 =控制邏輯模組 1〇0 2 (觸媒進料器# 2的進料區塊數目）。 實數輸出:R〇0 1 =輸入到上游Ρ Γ D (防止終止 )的F Β Κ (反饋）參數的R ρ Μ値。 -72- 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） 523647 A7 B7 五、發明説明（70) 本文所引用的所有的專利、檢驗程序、和其他文獻包 括先前引用的文獻都以參考的形式全部倂入本文’並且其 —城a 鄉可範圍之內。 內容與本發明一致，其引用的許可權皆€# (請先閲讀背面之注意事項再填寫本頁) 經濟部智慧財產局員工消費合作社印製 -73- 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐）523647 A7 B7 V. Description of the invention (Remote given command; B 0 0 3 = "〇, means" start "* Can run advanced control program '1' shows that at least one attack can accept the given command, and the advanced control program is ready to run. B〇〇4 = — B ◦ (;) 3 RP M shunting logic printed by the employee's consumer cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs _ practice A_: R 1 0 1 = output of low signal selector (not shown in LOSEL); Ri 〇2 = Current feeder # 疋 値, RI 0 3 2 The current # 2 feeder r ρ μ given 给 a gas level soap Λ,: Β 1 〇1 = D c of the control logic module 〇〇1 (such as "0 shows feeder #i is not ready to accept remote control. Such as" 1 "shows feeder # 丨 is ready to accept remote setpoint." BI 〇2, etc. = b of the DCS control logic module 2 (For example, it is shown that feeder # 2 is not ready to accept remote setpoints. For example, "1" Feeder # 2 is ready to accept remote setpoints.) BI〇3 = B〇0 3 of the DC logic module ("〇" Means "Enable" and cannot control the program. "1" means that at least one module can accept remote control and can open the advanced control program.) Input: II 〇1 = DCS control logic module I (number of feeding blocks for catalyst feeder # 1); II 0 2 = control logic module I ◦ 0 2 (feed for catalyst feeder # 2 Material area (given at the 6th end) "0", display control is transferred to high-end reference 0 0 1 DCS block number real number output: R 0 1 = RPM in automatic remote mode RP Μ adjusted by the rate controller-can be transmitted to the remote setpoint ®); R002 = RP Μ 値 in manual and short range mode (not applicable to the Chinese National Standard (CNS) Α4 specification (21 〇 > < 297 mm) -70-{Please read the precautions on the back before filling this page} 523647 A7 -------- B7____ 5. Description of the invention (d. RP Μ adjusted by the rate controller -Do not download the remote setpoint from below); R〇0 3 = R PF given rate of the feeder # 1 rate conversion module; (Please read the precautions on the back before filling this page) R〇0 42 Feeder # 2 is given by R P M of the rate conversion module. Integer variable: M 0 1 = Feeder # 1 The RPM is under operator control (RP M P ID is in manual or short range mode); Μ 0 2 = Feeder # 1 RPM is under operator control (RPM P ID is in manual or short-range mode) 値 Processing logic 1 input: RI 0 1 = CW valve maximum allowable boundaryCW; RI 0 2 = Condensation The maximum allowable weight percentage is RI 0 3 = the current CW valve position; RI 0 4 = the current condensate weight percentage; R 1 05 = the desired production rate given; RI 0 6 the current production rate; RI 〇 7 = Purge box water level given; r I 〇2 2 The current purge box water level given is printed by the consumer co-operative society of the Intellectual Property Bureau of the Ministry of Economic Affairs. Binary input: BI 〇2 CW valve position P ID tag name VALV C Manual / automatic mode (manual = 0, automatic = 1); BI 02 = VALVC's short-range / far-end (automatic / PCAS) mode; BI 〇3 = VALVC's startup state (tracking) (start-up 1 'not started = 〇); BI04 = Condensate weight percentage p ID tagname WCONC's manual / automatic mode (manual = 0, automatic = 1); 6 105 = boundary (: 〇 ^ (: short-range / far-end (automatic / PCAS) mode; BI 〇6 = WC〇NC startup status (tracking) (start = 1, not start = 〇); BI〇7 = speed RATE CONTROL-71-This paper size applies Chinese National Standard (CNS) A4 specification (210X297 mm) 523647 Α7 _ Β7 V. Description of the invention (6¾ (Please read the notes on the back before filling this page) Manual / automatic mode (manual 20 auto = 1); BI〇8 = short range / distal (auto / PCAS) mode of PRATC; Β I 〇9 = start state of PRatc (tracking) (start = 1, not Start two 0); Β I 丨 〇 = Manual / Auto mode of purge tank water level P ID tagname P BNL C (Manual = 0, Automatic = 1); biii = Proximity / Remote (Automatic / PCAS) of pbnlc Mode; BIO09 = Activation state (tracking) of PBNLC (Enable = 1, Not-enable = 〇). Real number output: R〇0 1 ^ CW valve position p I d tag name VALV C given 値; R 〇 02 = condensate weight percentage ρ I d labeled g own name WC 〇 NC given 値; R 〇 03 = rate control ρ ID is given by the name PRATC; 〇04 = purge tank water level ρ ID is given by the name PBNLC. M Anti-stop termination data: Huang 0: RI given by feeder # 1; RI 0 2 = given by current feeder p # of feeder # 2; employee of Bureau of Intellectual Property, Ministry of Economic Affairs Printed by consumer cooperatives RI 0 3 = output of low-signal selector tagname LOSELSEL (see Figure 7). Whole 1: Input: II 〇1 = Control logic module I 0 0 1 (catalyst feeder # 1 Number of feed blocks); II 〇2 = control logic module 002 (number of feed blocks of catalyst feeder # 2). Real output: R〇0 1 = input to upstream P Γ D ( F κ (Feedback) parameter R ρ Μ 値 for preventing termination) -72- This paper size is applicable to Chinese National Standard (CNS) A4 specification (210X297 mm) 523647 A7 B7 V. Description of Invention (70) All patents, inspection procedures, and other documents, including previously cited documents, are incorporated herein by reference in their entirety, and are within the limits of the city and the country. The content is consistent with the present invention, and the license rights of the references are all # (Please read the notes on the back before filling this page) Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs- 73- This paper size is applicable to China National Standard (CNS) A4 (210X297 mm)