TW201739508A - 使用先進多變數控制器控制阿法必妥(alphabutol)單元 - Google Patents
使用先進多變數控制器控制阿法必妥(alphabutol)單元Info
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- TW201739508A TW201739508A TW105139617A TW105139617A TW201739508A TW 201739508 A TW201739508 A TW 201739508A TW 105139617 A TW105139617 A TW 105139617A TW 105139617 A TW105139617 A TW 105139617A TW 201739508 A TW201739508 A TW 201739508A
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- Prior art keywords
- flow rate
- catalyst
- pressure
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- butene
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- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 claims abstract description 57
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 23
- 239000005977 Ethylene Substances 0.000 claims abstract description 23
- 238000004519 manufacturing process Methods 0.000 claims abstract description 17
- 239000007791 liquid phase Substances 0.000 claims abstract description 8
- 239000002815 homogeneous catalyst Substances 0.000 claims abstract description 6
- 239000003054 catalyst Substances 0.000 claims description 66
- 238000004886 process control Methods 0.000 claims description 28
- 230000008859 change Effects 0.000 claims description 25
- 238000006243 chemical reaction Methods 0.000 claims description 22
- 230000009471 action Effects 0.000 claims description 21
- 238000000034 method Methods 0.000 claims description 19
- 230000008569 process Effects 0.000 claims description 16
- 230000000694 effects Effects 0.000 claims description 12
- 239000000110 cooling liquid Substances 0.000 claims description 7
- 229920000642 polymer Polymers 0.000 claims description 7
- 230000004048 modification Effects 0.000 claims description 6
- 238000012986 modification Methods 0.000 claims description 6
- 230000015572 biosynthetic process Effects 0.000 claims description 5
- 230000004044 response Effects 0.000 claims description 4
- 238000012360 testing method Methods 0.000 claims description 3
- 230000003606 oligomerizing effect Effects 0.000 claims description 2
- 238000006384 oligomerization reaction Methods 0.000 abstract description 8
- 238000004821 distillation Methods 0.000 description 5
- 238000011084 recovery Methods 0.000 description 5
- 238000005194 fractionation Methods 0.000 description 4
- 239000012071 phase Substances 0.000 description 4
- 239000003060 catalysis inhibitor Substances 0.000 description 3
- 239000000498 cooling water Substances 0.000 description 3
- 239000003112 inhibitor Substances 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 2
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 2
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 2
- 229910052719 titanium Inorganic materials 0.000 description 2
- 239000010936 titanium Substances 0.000 description 2
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 239000011651 chromium Substances 0.000 description 1
- 238000005094 computer simulation Methods 0.000 description 1
- 230000003750 conditioning effect Effects 0.000 description 1
- 238000011217 control strategy Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000006471 dimerization reaction Methods 0.000 description 1
- 238000011143 downstream manufacturing Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 230000001360 synchronised effect Effects 0.000 description 1
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- VOITXYVAKOUIBA-UHFFFAOYSA-N triethylaluminium Chemical compound CC[Al](CC)CC VOITXYVAKOUIBA-UHFFFAOYSA-N 0.000 description 1
- 238000004148 unit process Methods 0.000 description 1
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Abstract
本發明描述一種用於藉由乙烯在均相催化劑存在下、在液相中且在起泡點之低聚合生產1-丁烯之單元的控制系統,其使用多變數預測性控制器且向該等單元提供較佳穩定性。
Description
本發明係關於先進製程控制APC及工業單元調整之領域。更具體而言,其係關於在均相催化劑存在下、在液相中且在起泡點操作之低聚合單元,催化劑可溶於反應相中。較佳地,根據本發明之製程適用於以乙烯為起始物質生產1-丁烯之低聚合製程。
專利EP 2 239 639 B1描述用於監測及調整對於單元之操作參數採用封閉迴路辨識相位之工業單元的方法。彼方法藉助於多變數控制器實施。 在本發明中,單元藉由動態模型建模,其中三個目標變數為丁烯生產率、反應器之溫度及壓力,且四個作用變數為饋料之流動速率、供應至一或多個催化劑再循環迴路之交換器的冷卻水的流動速率、及催化劑之兩個組分的兩個流動速率,或同樣地,催化劑之一種組分的流動速率及催化劑之彼組分的流動速率與另一組分之流動速率之間的比率。 在無APC之情況下,亦即根據先前技術,用於調整用於藉由乙烯低聚合生產1-丁烯之單元的常見模式可視單元而變化: - 在第一調整模式中,催化劑之流動速率的比率T2/LC保持固定,且催化劑之組分T2或LC的流動速率可變。通常,調節組分T2之流動速率以便控制單元之產率。在彼調整模式中,並不人為地修改乙烯之流動速率,因為其與反應器壓力控制級聯。術語「級聯」意指相比於作用變數(Vact)直接起作用以維持目標變數(Vtar)之簡單PID調整,目標變數(Vtar)藉由自身在另一個作用變數(Vact2)之控制下的另一個目標變數(Vtar2)保持恆定之事實。 - 在第二調整模式中,修改催化劑之流動速率的比率T2/LC以便控制1-丁烯之產量。乙烯流動速率與反應器之壓力控制級聯。 操作員一般藉由使催化劑之各組分的流動速率逐步變化來繼續進行,每一步對應於一個百分比點,一般在3%至20%之範圍內,更佳在5%至12%之範圍內,以便限制反應器中之壓力波動。 催化劑之流動速率的變化在單元之反應器中造成相對快速的效果,但由於在單元中之總體停留時間超過數小時,故必需等待在3小時至10小時範圍內之一段時間(視情況而定),以便在單元出口處辨別此等變化的效果。可使用一種先進控制系統克服此困難。 視單元而定,可存在一至三個催化劑再循環迴路。在上文所述之兩個調整模式中,藉由作用於供應至一或多個催化劑再循環迴路之一或多個交換器的冷卻液體的流動速率來使溫度保持恆定。大部分低聚合反應亦導致形成能夠沈積於低溫區且特定言之交換器中之聚合物,其引起交換係數之變化及功效降低。
實施本發明之先進製程控制,亦即具有APC,意指可進行多變數調整,藉助於此,反應器溫度(Treac)、反應器壓力(Preac)及因此單元之產率(Dprod)更加穩定。 根據本發明之製程使用多變數控制器。用於藉由乙烯之低聚合生產1-丁烯的製程的動態建模已意指可確定新穎先進控制策略,其將在下文稱作「本發明之先進製程控制」,其實質上不同於習知地經採用以操作此類型之單元的策略。 根據本發明,意欲保持恆定、稱為目標變數之3個參數為反應器壓力(Preac)、反應器溫度(Treac)及所生產之1-丁烯的流動速率(Dprod)。 為了保持目標變數恆定而所作用於之4個作用變數為:乙烯流動速率(Dch)、兩個催化劑組分(T2及LC)之流動速率及供應至催化劑再循環迴路之一或多個交換器的冷卻液體的流動速率。 更精確而言,本發明之先進製程控制(APC)使用多變數控制器(稱為APC控制器),其係基於3個原理: - 藉由作用於饋料流動速率(Dch)使經注入催化劑(T2或LC)之數量變化來控制反應器壓力(Preac),以便補償壓力對於影響產物流動速率(Dprod)之轉化率的效果, - 藉由作用於催化劑流動速率(LC或T2)而由饋料流動速率來控制產物流動速率(Dprod),以便補償對於壓力之效果, - 藉由作用於供應至一或多個催化劑再循環迴路之一或多個交換器之冷卻液體的流動速率來控制反應器溫度(Treac)。 APC控制器安裝在連接至控制工業單元中之製程的系統的電腦中,該電腦執行以下操作: - 恢復作用變數及目標變數之信號, - 生成作用變數之新設定點,以及 - 將新設定點傳送至製程控制系統。 根據本發明之先進製程控制的第一變化,催化劑之兩個組分的比率T2/LC為固定的且僅作用於組分T2之流動速率。在此情況下,比率(T2/LC)保持在1.5莫耳/莫耳與3莫耳/莫耳之間,更具體而言在1.9莫耳/莫耳與2.5莫耳/莫耳之間,且極佳在2莫耳/莫耳與2.2莫耳/莫耳之間,以便限制聚合物之形成。 根據本發明之先進製程控制之一變化,催化劑T2及LC之流動速率在一範圍內自由變化,使得比率(T2/LC)保持在1.5莫耳/莫耳與3莫耳/莫耳之間,更具體而言在1.9莫耳/莫耳與2.5莫耳/莫耳之間,且極佳在2莫耳/莫耳與2.2莫耳/莫耳之間,以便限制聚合物之形成。 在本發明之先進製程控制的一常規功能模式中: - 當壓力設定點變化時,在恆定產量下,修改催化劑之組分的流動速率以便控制壓力之變化,且饋料流動速率之修改補償由新壓力設定點產生之轉化率(及因此產量)的變化, - 當產量設定點變化時,在恆定壓力下,修改饋料流動速率以便控制產量之變化,且催化劑之兩個組分的流動速率的修改補償由新產量設定點產生之壓力變化的效果。 為獲得本發明之先進製程控制,藉由獲得實驗資料預先進行該先進製程控制之參數化,該實驗資料來源於由在作用變數中產生變化組成之測試的操作且在單元對於目標變數之回應之後,作用變數中之變化及目標變數之回應在多變數辨識軟體中經處理。 本發明亦關於針對用於乙烯之低聚合以便產生1-丁烯之製程的先進製程控制的應用,該製程較佳在以下條件下操作: - 壓力在0.5 MPa至8 MPa之範圍內,較佳在1 MPa至4 MPa之範圍內, - 溫度在20℃至150℃之範圍內,較佳在30℃至100℃之範圍內。 可用於本發明之製程中的催化劑已例如描述於專利文獻EP-A-2 388 069及EP-B-0 885 656中;其描述以引用之方式併入本文中。 較佳地,催化劑包含基於鈦或鉻、更佳基於鈦之第一組分,及基於鋁之第二組分。
為充分理解本發明,應回顧用於在反應器中、在液相中在起泡點在均相催化劑存在下操作之乙烯低聚合成1-丁烯之製程的功能。 在工業單元中,當已恰當調節反應器中之溫度及液相之層級時,至關重要的是控制兩個其他參數: - 反應器壓力,其必須保持在設計規格內或經歷選擇率之較大損失, - 1-丁烯產量,其必須適於下游製造單元之要求。 在本發明之先進製程控制中(具有APC),在多變數預測性控制器中使用動態模型意味著可採用以下由下文之封閉迴路動態模擬說明之策略: - 藉由作用於饋料流動速率使經注入催化劑之數量變化來控制反應器壓力,以便補償壓力對於影響產量之轉化率的效果。 - 藉由作用於催化劑之數量而由饋料流動速率來控制產量,以便補償對於壓力之效果。 - 藉由作用於供應至一或多個催化劑再循環迴路之一或多個交換器之冷卻液體的流動速率來控制溫度。 在聚合物沈積於一或多個迴路交換器中之情況下,先進製程控制之多變數控制器亦可用於預測彼等交換器之功效的降低。 作為說明在此處給出之根據本發明之APC方法的模擬的一個實例可由以下點概述(在下文描述中出現之編號係參考圖5給定): - 當壓力設定點(1)變化時,在恆定產量下,修改催化劑之組分的流動速率(2)以便控制壓力之變化。此外,饋料流動速率(3)之修改補償由新壓力設定點(4)產生之轉化率(及因此產量)的變化, - 當產量設定點(5)變化時,在恆定壓力下,修改饋料流動速率(6)以便控制產量之變化,且催化劑之流動速率(7)的修改補償由新產量設定點(8)產生之壓力變化的效果。 在此實例中,未呈現溫度控制。轉化中之任何變化影響放熱性及因此反應器之溫度,且因此將調節冷卻水之流動速率。 藉由使用APC: - 調整催化劑流動速率意味著可使影響壓力之擾動減至最少。壓力為穩定的。 - 饋料流動速率及相關產量為穩定的。 - 由於已預料一或多個交換器之功效損耗,故與使用習知調整系統相比溫度更加穩定。 在本發明之調整系統(稱為APC系統)中,採用存在於乙烯饋料流動速率與1-丁烯產物流動速率之間的直接比例聯繫。用於生產 1 - 丁烯之製程的描述
圖1呈現用於以乙烯為起始物質生產1-丁烯之製程之典型佈局的原理。 製程包含由基本上包含乙烯之饋料(1)供應之反應器(C1)。反應器(C1)亦由包含兩個組分(LC及T2) (其藉由各別流3及2分別引入至反應區中)之均相催化劑懸浮液供應。 乙烯在液相中之催化性二聚合在0.5 MPa至8 MPa範圍內、較佳1 MPa至4 MPa範圍內之壓力下,及在20℃至150℃範圍內、較佳30℃至100℃範圍內之溫度下操作。 由於反應為放熱的,故藉助於在包含水交換器(未顯示於圖1中)(其具有水作為冷卻液體)之迴路中冷卻流出物之一部分來調整反應器中之溫度。 隨後使來自反應區之流出物(4)與催化劑回收區(CR)中之催化劑抑制劑接觸。線路(6)對應至催化劑抑制劑。任何催化劑抑制劑可用於本發明之製程中,特定言之描述於專利FR 2 733 497中之彼等催化劑抑制劑。使抑制劑流(4)引入至催化劑回收區中且回收廢催化劑流(5)。 在(7)處使經濃縮催化劑溶液與無催化劑反應流出物分離且將該流出物(7)傳送至包含第一管柱(C2)之分餾區,其可用於分離頂部未經轉化之乙烯(8),再循環至反應區,及底部流出物之剩餘部分(10),供應至第二分離管柱(C3)。 第二分餾管柱(C3)可用於使基本上包含1-丁烯(11) (其為所需產物)之餾分與較重寡聚物(由流(12)表示)分離。先進製程控制 ( APC ) 之描述
本發明之先進製程控制(下文稱為APC)一般而言可在液相中且在起泡點下、以氣態饋料為起始物質、使用可溶於液相中之催化劑(均相催化劑)操作之任何單元中進行。 在本發明之先進製程控制中,操作員界定目標變數值,且APC將所有作用變數考慮在內;操作員不再需要關注作用變數。可應用此策略以便獲得在操作期間單元之較佳穩定性。 藉由獲得實驗資料預先進行先進製程控制之參數化。此等實驗資料來源於由在作用變數中產生變化組成之測試的操作。隨後在多變數辨識軟體中處理單元對於目標變數之回應。因此,舉例而言,獲得時延,其對應於在操控作用變數之時刻與開始對於目標變數回應之間經過的時間;可獲得時間常數及增量,其共同定義考慮作用變數之設定點之變化的目標變數之變化的動力學。 藉由操控流動速率控制器控制反應器溫度(Treac)。量測其檢驗反應器底部之溫度處於目標(或處於設定點)。 亦控制在反應器(C1)中包含催化劑之液體再循環迴路(在此項技術中稱為泵唧循環)中交換器(未顯示於圖1中)的入口溫度。 對氣相再循環之分析可用於測定存在之乙烯及1-丁烯的量。 藉由作用於催化劑之組分LC及T2之流動速率或藉由調整LC之流動速率及比率T2/LC兩者來控制反應器壓力(Preac)。 每通過一次之轉化率一般保持在低於90%,較佳低於87%,以便限制形成聚合物之風險。 藉由作用於每通過一次之轉化率及乙烯入口流動速率來控制產量。 作用變數可用於同時且連續控制目標變數,在不使用APC之情況下其為不可能的,因為簡單PID控制不會恰當運行以使視多參數而定之目標變數穩定。 另外,所生產之1-丁烯的流動速率(Dprod)與進入的乙烯饋料流動速率成比例,且因此其操縱以控制反應器壓力(Preac)與控制產物流動速率(Dprod)相反。只有藉由使用多變數APC可獲得所有目標變數之同步及連續控制。本發明之實例
根據圖1之佈局藉由乙烯之低聚合生產1-丁烯的工業單元配備有本發明之先進製程控制系統,該先進製程控制系統具有本說明書中所提及且圖1所展示之控制器。 藉由在2.1 MPa及在52℃下操作反應器,使用由AXENS出售之LC2253作為催化劑的第一組分及TEA (三乙基鋁(C2
H5
)3
Al,稀釋於正己烷中)作為催化劑的第二組分,單元生產3.0 t/h之1-丁烯。此比率較佳保持在1.5莫耳/莫耳與3莫耳/莫耳之間,更佳在1.9莫耳/莫耳與2.5莫耳/莫耳之間且極佳在2莫耳/莫耳與2.2莫耳/莫耳之間,以便限制聚合物形成。 APC控制器安裝在連接至工業單元製程控制系統之電腦上。電腦恢復作用變數及目標變數之信號,生成新作用變數設定點且將其傳送至製程控制系統。 圖2展示先進控制系統可用於極有效地調整反應器底部溫度,其中在先進控制存在下此底部溫度之變化與不具有先進控制之單元相比小4倍。 圖3展示反應器壓力之極佳調整,此壓力之值隨時間之變化的範圍顯著降低,此係因為與使用先前技術調整系統獲得之值相比,關於目標值之變化降低了6倍。 圖4表示反應器壓力及1-丁烯產物流動速率隨時間之變化隨饋料流動速率及兩個催化劑之流動速率而變化。 右手側圖像係根據本發明,亦即在APC之應用下,且左手側圖像係根據先前技術。 - 在無APC調整之系統下,可看出操作員僅操縱饋料流動速率,且僅在小程度上操縱催化劑流動速率。催化劑1之流動速率保持幾乎恆定。他必須在控制產物流動速率與控制反應器壓力之間作出妥協。 - 在APC調整系統下,可看出饋料流動速率及兩個催化劑經同時且連續地操控,以便控制產物流動速率及反應器壓力。亦可看出(且此為本發明之系統的主要優點)產物流動速率及反應器壓力更加有效地受控,亦即各自保持非常接近於設定點。 圖5展示兩個作用變數之作用:饋料流動速率(指示3隨後6)及兩個催化劑流動速率之間的比率(指示2隨後7),以便操作兩個目標變數之設定點的變化:丁烯之產物流動速率(指示5隨後8)及反應器壓力(指示1隨後4)。 關於兩個目標變數(亦即1-丁烯之產量及反應器壓力)之兩個變化由以下負責: - 藉由饋料流動速率變數,開始極緩慢升高(指示3),隨後其次更快升高(指示6), - 藉由催化劑之比率的變數,開始此值降低(指示2),隨後其次值升高至與起始值實質上相同程度(指示7)。
1‧‧‧壓力設定點/饋料 2‧‧‧催化劑之組分的流動速率/T2流 3‧‧‧饋料流動速率/LC流 4‧‧‧新壓力設定點/來自反應區之流出物/抑制劑流 5‧‧‧產量設定點/廢催化劑流 6‧‧‧饋料流動速率/線路 7‧‧‧催化劑之流動速率/無催化劑反應流出物 8‧‧‧新產量設定點/未經轉化之乙烯 10‧‧‧流出物之剩餘部分 11‧‧‧1-丁烯 12‧‧‧寡聚物流 C1‧‧‧反應器 C2‧‧‧蒸餾管柱/第一管柱 C3‧‧‧蒸餾管柱/第二分離管柱/第二分餾管柱 CR‧‧‧催化劑回收區 E1‧‧‧水交換器/交換器 LC‧‧‧催化劑組分 T2‧‧‧催化劑組分
圖1表示用於乙烯低聚合成1-丁烯之製程的佈局,其中突出主流、反應器(C1)及兩個蒸餾管柱(C2及C3)。此佈局亦展示本發明之控制及調整系統的主要元件,亦即用於控制或調整作用變數(單元之饋料的流動速率、各催化劑之流動速率、冷卻水之流動速率)及目標變數(反應器壓力、產物流動速率、反應器溫度)之系統。 圖2表示單元之反應器溫度的變化隨時間而變的兩個直方圖。圖2a之圖像係根據本發明,亦即在APC之應用下,且圖2b之圖像係根據先前技術。可觀測到具有APC調整系統之值的離散極大降低。 圖3表示反應器壓力隨時間之變化的兩個直方圖。圖3a之圖像係根據本發明,亦即在APC之應用下,且圖3b之圖像係根據先前技術。可觀測到具有APC調整系統之值的離散極大降低。 圖4表示反應器壓力(指示4)及1-丁烯產物之流動速率(指示5)隨時間之變化隨饋料流動速率及催化劑之兩個組分的流動速率(分別對於T2指示2及對於LC指示3)而變化。 右手側圖像係根據本發明,亦即在APC之應用下,且左手側圖像係根據先前技術。在右手側圖像將觀測到兩個目標變數之顯著穩定:反應器壓力及1-丁烯產量。 圖5展示兩個作用變數饋料流動速率(指示3隨後6)及兩個催化劑流動速率之間的比率(指示2隨後7)如何起作用以實現以下兩個目標變數之設定點的變化:丁烯產物流動速率(指示5隨後8)及反應器壓力(指示1隨後4)。
1‧‧‧饋料
2‧‧‧T2流
3‧‧‧LC流
4‧‧‧來自反應區之流出物/抑制劑流
5‧‧‧廢催化劑流
6‧‧‧線路
7‧‧‧無催化劑反應流出物
8‧‧‧未經轉化之乙烯
10‧‧‧流出物之剩餘部分
11‧‧‧1-丁烯
12‧‧‧寡聚物流
C1‧‧‧反應器
C2‧‧‧蒸餾管柱/第一管柱
C3‧‧‧蒸餾管柱/第二分離管柱/第二分餾管柱
CR‧‧‧催化劑回收區
Claims (6)
- 一種先進製程控制(APC),其可應用於在均相催化劑存在下、在液相中且在起泡點操作之乙烯至1-丁烯之低聚合的單元,其特徵在於同時且連續受控、稱為目標參數之該等參數為1-丁烯之產量(Dprod)、反應器壓力(Preac)及反應器溫度(Treac),且作用變數為饋料流動速率(Dch)、經注入催化劑之組分(T2及LC)中之每一者的流動速率及供應至一或多個催化劑再循環迴路之一或多個交換器之冷卻液體的流動速率。
- 如請求項1之先進製程控制(APC),其中該先進製程控制之多變數控制器(稱為APC控制器)係基於3個原理: 藉由作用於該饋料流動速率使經注入催化劑之數量變化來控制該反應器壓力(Preac),以便補償壓力對於影響該產量之轉化率的效果, 藉由作用於催化劑之該數量而由該饋料流動速率來控制該產量(Dprod),以便補償對於該壓力之效果, 藉由作用於供應至該一或多個催化劑再循環迴路之該一或多個交換器之冷卻液體的該流動速率來控制該反應器溫度(Treac), 該APC控制器係安裝在連接至控制該工業單元中之製程的系統的電腦中,該電腦執行以下操作: 恢復該等作用變數及該等目標變數之信號, 生成該等作用變數之新設定點,以及 將該等新設定點傳送至該APC控制器。
- 如請求項2之先進製程控制,其中該等催化劑T2及LC之該等流動速率在一範圍內自由變化,使得比率(T2/LC)保持在1.5莫耳/莫耳與3莫耳/莫耳之間,更具體而言在1.9莫耳/莫耳與2.5莫耳/莫耳之間,且極佳在2莫耳/莫耳與2.2莫耳/莫耳之間,以便限制聚合物之形成。
- 如請求項1之先進製程控制,其中: 當該壓力設定點變化時,在恆定產量下,修改該催化劑之組分的流動速率以便控制該壓力之變化,且該饋料流動速率之修改補償由該新壓力設定點產生之轉化率及因此1-丁烯產量之變化, 當該產量設定點變化時,在恆定壓力下,修改該饋料流動速率以便控制產量(亦即1-丁烯之該流動速率)之變化,且該催化劑之兩個組分的流動速率的修改補償由該新產量設定點產生之該壓力變化的效果。
- 如請求項1之先進製程控制,其中藉由獲得實驗資料預先進行該先進製程控制之參數化,此等實驗資料來源於由在該等作用變數中產生變化組成之測試的操作,且該單元對於該等目標變數之回應在多變數辨識軟體中經處理。
- 一種如請求項1至5中任一項之先進製程控制針對乙烯低聚合以便產生1-丁烯之製程的應用,該製程係在以下條件下操作: 壓力在0.5 MPa至8 MPa之範圍內,較佳在1 MPa至4 MPa之範圍內, 溫度在20℃至150℃之範圍內,較佳在30℃至100℃之範圍內。
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