201041793 六、發明說明： 【發明所屬之技術領域】 [0001]本發明涉及一種笨二甲酸（TAC，Terephthalic Acid) 生產工藝中的粉體輪送系統及其使用方法，具體地涉及 一種粗製苯二甲酸粉體輪送系統及其使用方法。 [先前技術]201041793 VI. Description of the Invention: [Technical Field] [0001] The present invention relates to a powder transfer system in a production process of TAC (Terephthalic Acid) and a method of using the same, and in particular to a crude benzene Formic acid powder delivery system and method of use thereof. [Prior technology]
[0002]此處先簡單地介紹現有的精製苯二甲酸（簡稱為PTA)工 藝段的工藝流程’苯二甲酸包括對苯二甲酸及間苯二甲 酸’兩者精製工藝基本相同，現以精製對苯二曱酸生產 流程為例以說明。現多數的精製工藝段採用類似的 處理方法來進行對笨二曱酸提純、.，典型.步棘如下： _ h 酸卫藝段所反麟到观料在通過分離 機刀離之後進入乾燥機乾燥，乾燥後的粉體經由回轉閥 後通過氣體輸送、鏈鬥輸送或其他方式輪送到粗製對苯 二甲酸儲料倉中。 [0004] 2.粗 _ 料 # m T本一甲酸儲料倉中的粉體經由回轉閥後再通過 f旋輪送器或其他方式輸送到衆化槽中，也有將粗製對 奸甲竣粉體由乾燥機出料口經由回轉閥後通過氣體輸 鍵鬥輪送或其他方式直接輸送到漿化槽中。 [0005][0002] Here is a brief introduction to the existing process process of refined phthalic acid (referred to as PTA) process section. The purification process of phthalic acid including terephthalic acid and isophthalic acid is basically the same, and now it is refined. The benzoic acid production process is exemplified. Most of the refining process sections use a similar treatment method to purify the stupid acid. The typical step is as follows: _ h The acid weiyi section is used to enter the dryer after passing through the separator. The dried, dried powder is transferred to the crude terephthalate storage silo via a rotary valve and then by gas delivery, bucket conveyor or other means. [0004] 2. The raw material in the crude formic acid storage silo is transferred to the publicized tank through the rotary valve after the rotary valve or other means, and there is also a coarse powder on the beetle. The body is directly conveyed to the pulping tank by the dryer discharge port through the rotary valve and then through the gas transfer button or other means. [0005]
酸粉體與來自精製苯二甲酸精製段的回 &或者部分新鮮純水在攪拌機作用下攪拌得到所需濃 度的漿料 Μ ’其濃度一般在23%到30%之間； 搜掉後的漿料經加壓泵、高壓泵逐步加壓後，進入多 段加熱H tb 、 甲’逐步升溫、溶解，直到進入氫化反應器， 098116488 表單鳴號A〇i〇1 第3頁/共14頁 0982027941-0 [0006] 201041793 此時漿料已完全溶解。 [0007] 5.氫化反應器中，通過還原反應將不純物還原為易分離 的不純物來純化對苯二甲酸。 [0008] 6.反應完成之後進入結晶罐結晶，得到精製對苯二甲酸 的新漿料。 [0009] 7.得到的新漿料通過輸送泵進入固液分離工藝段，分離 工藝段分為一段式、兩段式或多段式幾種。在典型的兩 段式工藝中，後段分離工藝的分離機所產出的母液將被 回收，通過回收水槽收集，利用回收水泵輸送回漿化槽 中，作為步驟3中的漿化水。 [0010] 8.分離出來的精製對苯二甲酸固體經乾燥機乾燥後進入 料倉儲存、包裝； [0011] 本發明主要針對前述步驟1和步驟2做了改進，即從乾燥 機出來的粗製苯二甲酸粉體輸入到料倉，再由料倉到漿 化槽這段工藝的改進。這段工藝現有的處理方式主要為 高壓氣送方式或鏈鬥式輸送方式兩種。若採用高壓氣送 方式，以年產100萬噸PTA的工廠為例，年操作時間為 8000小時，則回轉閥流量為125噸/小時，氣體輸送耗氣 量約為12. 5噸/小時，若氣體單價為55元/噸，則其年累 計費用為12. 5x55x8000 = 5，500，000元，能量消耗巨大 ;現有的鏈鬥式輸送方式也存在費用昂貴、不易維護的 問題，一旦鏈條損壞就需要較長的時間退鏈維修。 【發明内容】 [0012] 本發明的目的在於提供一種粗製苯二曱酸粉體輸送系統 098116488 表單編號A0101 第4頁/共14頁 0982027941-0 201041793 [0013] [0014]❹ [0015] [0016] Ο [⑻ 17] [0018] 098116488 ，以解決現有技術中存在的上述問題。本發明將粗製笨 二甲酸粉體輸送管道的全部或後段改為液體輪送管道， 使部分粗製苯二甲酸粉體不再通過高壓氣送管道或鏈鬥 輸送系統輸送，改為用水輸送，大大降低了能源的耗用 量。 本發明的另一目的在於提供前述粗製苯二甲酸粉體輪送 系統的使用方法。 本發明提供的技術方案如下： 一種粗製苯二甲酸粉體輸送系統，粗製苯二甲醆乾燥機 上設置有至少一個的出料口 ’其中至少有一個教製苯二 甲酸乾燥機出料口與漿化槽進料口連接的粗製笨二甲酸 輸送管道的全部或後段為液體輪送管道。 如此，從乾燥器到漿化槽的部分或全部鉅雞不再使用高 壓氣送系統或鏈鬥輸送系統輸送粉體，從而大大節約了 生產設備的投資，並降低了輸送過程中的能源耗用量。 所述的線上混合裝置可奴是現有的任何混合器，設置包 括與乾燥機出料口相關設備的組合。 前述粗製笨二甲酸粉體輸送系統中，所述液體輪送管道 包括一個設置在液體輸送管道進料口的線上混合裝置， 所述線上混合裝置包含有至少兩個的進料口和至少一個 的出料口》 前述粗製笨二甲酸粉體輸送系統中，粗製苯二甲酸乾燥 機設置有兩個帶有閥門的出料口，線上混合裝置設置有 兩個進料口和一個出料口，粗製苯二曱酸乾燥機的其中 表單編號Α0101 第5頁/共14頁 0982027941-0 201041793 一個出料口與線混合器的其中一個進料口連接，線上混 合裝置的另一個進料口與進水管相接，線上混合裝置出 料口通過接液體輸送管道與漿化槽連接；粗製苯二甲酸 乾燥機的另一個出料口通過高壓氣送管道或鏈鬥輸送系 統與料倉進料口相聯接。如此，粗製苯二曱酸粉體或通 過液體輸送系統、或通過氣體輸送系統、或通過鏈鬥輸 送系統進入漿化槽，隨意切換多種輸送方式。 [0019] 前述粗製苯二甲酸粉體輸送系統中，粗製苯二曱酸乾燥 機出料口通過高壓氣送管道或鏈鬥輸送系統與料倉進料 口相聯接，料倉出料口通過液體輸送管道和漿化槽進料 口相聯接。這樣，在漿化槽的後段工藝由於維修、保養 等原因處於停止狀態，而前段工藝繼續工作的情況下， 可以將從乾燥機出來的粗製苯二甲酸粉體輸送到料倉暫 時保存。 [0020] 前述粗製苯二甲酸粉體輸送系統的使用方法，其特徵在 於：從粗製笨二曱酸乾燥機或料倉出來的粗製笨二曱酸 粉體和從進水管流入的水進入液體輸送管道後，使用設 置在液體輸送管道進料口的線上混合裝置將粗製苯二曱 酸粉體和水混合成重量百分比濃度為20 %至40%漿料。 重量百分比濃度為20 %至40%的漿料的溶解性和流動性 良好，幾乎可以完全將粗製苯二曱酸粉體輸送到漿化槽 中，而後再在漿化槽内將漿料調整至後段工藝所需的濃 度。 [0021] 前述粗製苯二甲酸粉體輸送系統的使用方法中，漿料在 液體輸送管道中的流速大於或至少等於1. 5m/s，以防止 098116488 表單編號A0101 第6頁/共14頁 0982027941-0 201041793 漿料在輸送管道中滯留下來。 [0022] 前述粗製苯二甲酸粉體輸送系統的使用方法中，所述水 可以是新鮮的純水、粗製苯二甲酸工藝段的任何回收水 或其他不影響粗製苯二甲酸精製的流體。從而可以有效 地利用後段工藝的壓力分離機所得的回收水，可簡化流 程，降低耗水量。 [0023] 除非特別指名，這裏所使用的所有技術和科學術語的含 義與本發明所屬技術領域一般技術人員通常所理解的含 〇 義相同。同樣，所有在此提及的出版物、專利申請、專 利及其他參考資料均可以引入本發明作為參考。 [0024] 综上，本發明創造性的提供了一種粗製笨二曱酸粉體輸 送系統及其使用方法，將粗製苯二甲酸粉體輸送管道的 全部或後段改為液體輸送管道，使部分粗製苯二甲酸粉 體不再通過高壓氣送管道或鏈鬥輸送系統輸送，改為用 水輸送，大大降低了能源的耗用量。同時，重量百分比 & 濃度為23%至40%的漿料的溶解性和流動性良好，幾乎 〇 可以完全將粗製苯二甲酸粉體輸送到漿化槽中，而後再 在漿化槽内將漿料調整至後段工藝所需的濃度。 【實施方式】 [0025] 實施例1 [0026] 如第一圖中所示，粗製苯二曱酸乾燥機（1 )設置有兩個 帶有閥門（2)的出料口，線上混合裝置（5)為一設置 有兩個進料口和一個出料口的三通管件，粗製苯二曱酸 乾燥機（1)的其中一個出料口與線上混合裝置（5)的 098116488 表單編號A0101 第7頁/共14頁 0982027941-0 201041793 其中一個進料 的另一個進料 口連接，線上混合裝置（5 ) 口設置-增壓系⑷’並與進水管⑺相接，線上混， 合裝置（5)的出料口通過液體輪送管道（11)與聚化槽 ⑴連接；粗製笨二甲酸乾燥機⑴的另一出料口通 —㈣(⑴㈣倉U)進料σ相聯接，料倉 ⑷出料口通過螺旋輪送器（13)與聚化槽⑴進料、 口相聯接。 [0027] [0028] [0029] 098116488 這樣粗製苯—甲酸粉體或通過液體輸送管道（11)進 入漿化槽（3) ’或通過高壓氣送管道（12)進入漿化槽 (3)，兩種輸送方式可相互切換。 實施例2 /: 如第-圖中所示’粗製苯二曱酸乾燥機⑴設置有一個 帶有閥門（2)的出料口，線上混合裝置（5)為一設置 有兩個進料口和一個出料口的三通管件，粗製苯二甲酸 乾燥機（1)的出料口與線上混合裝置（5)的其中一個 進料口連接’線上混合震置（5)的另一個進料口設置一 '：!^ r ' 增壓泵（6)，並與進水管（？）連接，線上混合裝置（5 )的出料口通過接液體輸送管道（11)與漿化槽（3)連 接。某PTA生產廠家，pta產能為1〇〇萬噸/年，年操作時 間為8000小時’從乾燥機出來的流量為ία噸/小時的粗 製苯二甲酸粉體進入上述設置的液體輸送管道；同時， 通過進水管向液體輸送管道内輸入流量為415噸/小時的 水’用420m3/h、l〇mH、泵功率為2〇kw的增壓泵提高回 收水出料口壓力，以改善線上混合裝置（5)混合效果。 使用線上混合裝置（5)將粗製苯二甲酸粉體和的水直接 第8頁/共14頁 表單編號A0101 201041793 混合成漿料後輸入漿化槽（3)中，所述漿料的重量百分 比濃度為20%至40%，漿料在管道中的流速大於或至少 低於 1. 5m/s。 [0030] 為節約耗水量，本實施例中的漿化槽（3)的漿化用水絕 大部分來自後後段工藝的壓力分離機所得的回收水，一 小部分為補充的新鮮水。漿化水的使用總量與氣送方式 所用水量是相同的，本發明很好的利用的回收水的動能 做為混合制漿的能量。 1 Ο [0031] 換為水力輸送後，能耗主要由增壓泵產生，工業用電以 0. 7元/ kwh計算，其中，增壓泵的能耗為 20x8000x0. 7 = 1 1 2, 000元（年操作時間為8000h計算） [0032] 比較例 [0033] 某ΡΤΑ生產廠家，ΡΤΑ產能為100萬噸/年，年操作時間為 8000小時，乾燥機出料口處回轉閥流量為125噸/小時。 Ο 從粗製苯二甲酸乾燥機出來的粗製苯二曱酸粉體經由高 壓氣送系統輸送至料倉頂部，再從料倉經由高壓氣送系 統輸送至漿化槽中，其氣體輸送方式耗氣量為12.5噸/小 時，高壓氣體的價格以55元/噸計算，則粗製苯二甲酸粉 體從乾燥機輸送到漿化槽的年支出為：12.5噸/小時X 8000小時χ55元/噸二5, 500, 000元 ° [0034] 上述實施例為本發明較佳的實施方式，但本發明的實施 方式並不受上述實施例的限制，其他的任何未背離本發 明的精神實質與原理下所作的改變、修飾、替代、組合 098116488 表單編號Α0101 第9頁/共14頁 0982027941-0 201041793 、簡化，均應為等效的置換方式，都包含在本發明的保 護範圍之内。 【圖式簡單說明】 [0035] 第一圖為粗製苯二甲酸粉體輸送系統的結構示意圖。 [0036] 第二圖為另一種粗製苯二甲酸粉體輸送系統的結構示意 圖。 【主要元件符號說明】 [0037] ( 1 )粗製苯二甲酸乾燥機 [0038] ( 11 )液體輸送管道（12)高壓氣送管道 [0039] (13)螺旋輸送器 [0040] (2)閥門（3)漿化槽 [0041] (4)料倉（5)線上混合裝置 [0042] (6)增壓泵（7)進水管 098116488 表單編號A0101 第10頁/共14頁 0982027941-0The acid powder and the fresh & purified water from the purified phthalic acid refining section are stirred under the action of a mixer to obtain a slurry of the desired concentration Μ 'the concentration is generally between 23% and 30%; after the search After the slurry is gradually pressurized by the pressure pump and the high pressure pump, it enters the multi-stage heating H tb , A 'gradually heats up and dissolves until it enters the hydrogenation reactor, 098116488 Form horn A〇i〇1 Page 3 / 14 pages 098202794 -0 [0006] 201041793 The slurry is now completely dissolved. 5. In the hydrogenation reactor, terephthalic acid is purified by reducing the impurities to an easily separable impurity by a reduction reaction. [0008] 6. After completion of the reaction, the crystallizer was crystallized to obtain a new slurry of purified terephthalic acid. [0009] 7. The obtained new slurry enters the solid-liquid separation process section through the transfer pump, and the separation process section is divided into one-stage, two-stage or multi-stage. In a typical two-stage process, the mother liquor produced by the separator in the latter stage separation process is recovered, collected through a recovery tank, and transported back to the pulping tank using a recovery pump as the slurry water in step 3. [0010] 8. The separated purified terephthalic acid solid is dried in a dryer and then stored in a silo for storage and packaging; [0011] The present invention is mainly directed to the foregoing steps 1 and 2, that is, the crude from the dryer The process of inputting the phthalic acid powder into the silo and then from the silo to the pulping tank is improved. The existing treatment methods of this process are mainly high pressure gas delivery mode or chain bucket conveying mode. 5吨/小时, if the high-pressure gas delivery method is used, the annual production time is 8,000 hours, the rotary valve flow rate is 125 tons / hour, the gas delivery gas consumption is about 12. 5 tons / hour, if The unit price of gas is 55 yuan / ton, the annual cumulative cost is 12. 5x55x8000 = 5,500,000 yuan, the energy consumption is huge; the existing chain bucket conveying method also has the problem of expensive and difficult to maintain, once the chain is damaged It takes a long time to retreat the chain. SUMMARY OF THE INVENTION [0012] An object of the present invention is to provide a crude benzoic acid powder delivery system 098116488 Form No. A0101 Page 4 of 14 0982027941-0 201041793 [0013] [0014] 00 [0015] [0016] Ο [(8) 17] [0018] 098116488 to solve the above problems in the prior art. The invention converts all or the rear section of the crude doped dicarboxylic acid powder conveying pipe into a liquid wheel conveying pipe, so that part of the crude phthalic acid powder body is no longer transported through the high pressure gas conveying pipe or the chain bucket conveying system, and is changed into water conveying, which is greatly Reduce energy consumption. Another object of the present invention is to provide a method of using the aforementioned crude phthalic acid powder transfer system. The technical solution provided by the invention is as follows: A crude phthalic acid powder conveying system, wherein the crude phthalonitrile drying machine is provided with at least one discharge port, wherein at least one of the teaching phthalic acid dryer discharge ports and The entire or rear section of the crude succinic acid delivery pipe to which the slurry tank feed port is connected is a liquid transfer pipe. In this way, some or all of the giant chickens from the dryer to the pulping tank no longer use the high pressure gas delivery system or the chain bucket conveying system to transport the powder, thereby greatly saving investment in production equipment and reducing energy consumption during transportation. the amount. The in-line mixing device can be any existing mixer, and the combination includes a combination of equipment associated with the dryer discharge port. In the above crude dibenzoate powder delivery system, the liquid transfer conduit includes an in-line mixing device disposed at a feed port of the liquid delivery conduit, the in-line mixing device including at least two feed ports and at least one Discharge port In the above crude dibasic acid powder conveying system, the crude phthalic acid dryer is provided with two discharge ports with valves, and the on-line mixing device is provided with two feed ports and one discharge port, which are crude Form number of benzoic acid dryer Α0101 Page 5 of 14 0982027941-0 201041793 One discharge port is connected to one of the inlets of the line mixer, and the other inlet and inlet of the line mixing device In connection, the outlet of the on-line mixing device is connected to the pulping tank through the liquid conveying pipeline; the other outlet of the crude phthalic acid dryer is connected to the inlet of the silo through the high-pressure gas feeding pipeline or the chain bucket conveying system. . Thus, the crude benzoic acid powder can be switched into a slurry tank by a liquid delivery system, or by a gas delivery system, or by a chain conveyor system, and a plurality of conveying modes can be switched at will. [0019] In the above crude phthalic acid powder conveying system, the discharge port of the crude phthalic acid dryer is connected to the feed port of the silo through a high-pressure gas supply pipe or a chain bucket conveying system, and the discharge port of the silo passes through the liquid. The conveying pipe and the feed port of the pulping tank are connected. In this way, in the latter stage of the slurry tank, the process is stopped due to maintenance, maintenance, etc., and in the case where the previous stage process continues, the crude phthalic acid powder from the dryer can be transported to the silo for temporary storage. [0020] The method for using the crude phthalic acid powder delivery system described above, characterized in that the crude stearic acid powder from the crude bismuth diacid dryer or the silo and the water flowing in from the inlet pipe enter the liquid transport After the pipe, the crude benzoic acid powder and water are mixed into a 20% to 40% by weight slurry using an in-line mixing device disposed at the feed port of the liquid delivery pipe. The solubility and fluidity of the slurry having a concentration by weight of 20% to 40% is good, and the crude benzoic acid powder can be almost completely transported into the slurry tank, and then the slurry is adjusted to the slurry tank in the slurry tank. The concentration required for the latter stage process. [0021] In the method of using the crude phthalic acid powder delivery system, the flow rate of the slurry in the liquid delivery conduit is greater than or at least equal to 1. 5m / s, to prevent 098116488 Form No. A0101 Page 6 / 14 pages 098202794 -0 201041793 The slurry stays in the pipeline. [0022] In the method of using the crude phthalic acid powder delivery system, the water may be fresh pure water, any recovered water of the crude phthalic acid process section or other fluids that do not affect the purification of the crude phthalic acid. Therefore, the recovered water obtained by the pressure separator of the latter stage process can be effectively utilized, which simplifies the process and reduces the water consumption. [0023] Unless otherwise specified, all technical and scientific terms used herein have the same meaning meaning meanings Also, all publications, patent applications, patents, and other references mentioned herein are incorporated by reference. [0024] In summary, the present invention creatively provides a crude stupid acid powder conveying system and a method for using the same, and the whole or the rear section of the crude phthalic acid powder conveying pipe is changed into a liquid conveying pipe to make a part of crude benzene. The diformic acid powder is no longer transported through the high-pressure gas transmission pipeline or the chain bucket conveying system, and is transported by water, which greatly reduces the energy consumption. At the same time, the solubility and fluidity of the slurry with a weight percentage & concentration of 23% to 40% is good, and the crude phthalic acid powder can be completely transported into the pulping tank, and then in the pulping tank. The slurry is adjusted to the concentration required for the latter stage process. [Embodiment] [0025] Example 1 [0026] As shown in the first figure, a crude benzoic acid dryer (1) is provided with two discharge ports with valves (2), an in-line mixing device ( 5) For a tee fitting with two inlets and one outlet, one of the outlets of the crude benzoic acid dryer (1) and the mixing device for the line (5) 098116488 Form No. A0101 7 pages / total 14 pages 0982027941-0 201041793 One of the feed inlets is connected, the on-line mixing device (5) is set - the pressurized system (4)' and is connected to the inlet pipe (7), and the line is mixed and combined ( 5) The discharge port is connected to the polymerization tank (1) through the liquid transfer pipe (11); the other discharge port of the crude stearic acid dryer (1) is connected to (4) ((1) (four) bin U) feed σ phase connection, silo (4) The discharge port is connected to the feeding and mouth of the polymerization tank (1) through the spiral conveyor (13). [0029] [0029] [0029] 098116488 such crude benzene-formic acid powder or through the liquid delivery pipe (11) into the pulping tank (3) ' or through the high-pressure gas transmission pipe (12) into the pulping tank (3), The two transport modes can be switched to each other. Example 2 /: As shown in the figure - the crude benzoic acid dryer (1) is provided with a discharge port with a valve (2), and the in-line mixing device (5) is provided with two feed ports. And a three-way pipe fitting of the discharge port, the discharge port of the crude phthalic acid dryer (1) is connected with one of the inlet ports of the on-line mixing device (5), and the other feed of the on-line mixing device (5) The port is provided with a ':!^ r ' booster pump (6) and connected to the inlet pipe (?). The discharge port of the in-line mixing device (5) is connected to the slurry conveying pipe (11) and the slurry tank (3). connection. A PTA manufacturer has a pta capacity of 10,000 tons/year and an annual operating time of 8,000 hours. 'The crude phthalic acid powder with a flow rate of ία ton/hour from the dryer enters the liquid delivery pipe set above; Through the inlet pipe, the water with a flow rate of 415 tons/hour is input into the liquid conveying pipe. The pressure of the outlet of the recovered water is increased by the booster pump with 420m3/h, l〇mH and pump power of 2〇kw to improve the mixing on the line. The device (5) mixes the effect. The crude phthalic acid powder and the water are directly mixed into a slurry using an in-line mixing device (5), and then input into the slurry tank (3), and the weight percentage of the slurry is mixed into a slurry. 5米/斯。 The concentration of the slurry in the pipeline is greater than or at least less than 1. 5m / s. [0030] In order to save water consumption, most of the pulping water in the pulping tank (3) in the present embodiment comes from the recovered water obtained by the pressure separator of the latter stage process, and a small portion is the supplementary fresh water. The total amount of slurry water used is the same as that of the gas delivery mode. The kinetic energy of the recovered water which is well utilized in the present invention is used as the energy of the mixed pulping. 1 Ο [0031] After the hydraulic transmission, the energy consumption is mainly generated by the booster pump, and the industrial power is calculated at 0. 7 yuan / kwh, wherein the energy consumption of the booster pump is 20x8000x0. 7 = 1 1 2, 000 Yuan (annual operation time is calculated at 8000h) [0032] Comparative example [0033] A certain manufacturer has a production capacity of 1 million tons/year, an annual operation time of 8,000 hours, and a rotary valve flow rate of 125 tons at the discharge port of the dryer. /hour.粗 Crude phthalic acid powder from the crude phthalate dryer is transported to the top of the silo via a high-pressure gas delivery system, and then transported from the silo to the pulping tank via a high-pressure gas delivery system. For 12.5 tons / hour, the price of high pressure gas is 55 yuan / ton, the annual expenditure of crude phthalic acid powder from the dryer to the pulping tank is: 12.5 tons / hour X 8000 hours χ 55 yuan / ton 2 The embodiment is a preferred embodiment of the present invention, but the embodiment of the present invention is not limited to the above embodiment, and any other matter is not departing from the spirit and principle of the present invention. Changes, modifications, substitutions, combinations 098116488 Form No. Α0101 Page 9 of 14 0982027941-0 201041793 Simplifications, all equivalent equivalents, are included in the scope of the present invention. BRIEF DESCRIPTION OF THE DRAWINGS [0035] The first figure is a schematic structural view of a crude phthalic acid powder delivery system. [0036] The second figure is a schematic view of the structure of another crude phthalate powder delivery system. [Main component symbol description] [0037] (1) Crude phthalic acid dryer [0038] (11) Liquid delivery pipe (12) High pressure gas supply pipe [0039] (13) Screw conveyor [0040] (2) Valve (3) Slurry tank [0041] (4) Silo (5) on-line mixing device [0042] (6) Booster pump (7) Inlet pipe 098116488 Form No. A0101 Page 10 of 14 0982027941-0