3124平方甲醇合成反應(yīng)器的設(shè)計與制造（全套CAD圖+說明書+開題報告+翻譯）

3124平方甲醇合成反應(yīng)器的設(shè)計與制造（全套CAD圖+說明書+開題報告+翻譯）,平方,甲醇,合成,反應(yīng)器,設(shè)計,制造,全套,cad,說明書,仿單,開題,報告,講演,呈文,翻譯 外文翻譯1、英文原文Methanol distillation trays with high efficiency and process improvements in lineAbstract Brief description of the methanol distillation tower internals rehabilitation programs: micro-hole width efficient composite plate, more suitable than the regular packing, superior; analysis of three towers of methanol distillation tower process than the advantages of technology and economic benefits.Keywords Tray efficiency Process Route Improve For many chemical elements, the energy consumption of the technology is always an important factor in economic indicators. Save energy, reduce consumption and speed up the pace of technological transformation, the implementation of product structure adjustment, the survival of every business dispute, and development of important measures. Now after my factory technical transformation described by methanol distillation trays and improved high technology route to reducing energy consumption play an important role. Practice shows, for the methanol distillation separation, not just rely on highly efficient distillation column internals used in order to achieve significant reduction in energy consumption of alcohol distillation, and methanol distillation process improvements can be made to the system consumption decreased significantly.1 A methanol distillation tower process Currently, most of the twin towers of methanol distillation separation processes are used. My factory has a set of 3 104t / a methanol tower distillation unit, in December 2002 to be expanded to 8 104t / a methanol tower distillation unit, the process shown in Figure 1.This process constituted by the two distillation columns: pre-tower and the main tower. Come from the methanol synthesis section in the crude methanol containing 86% methanol, the first into the pre-tower, is actually a pre-column extractive distillation column, in the top of the tower by adding the equivalent of 20% crude methanol feed. 30% of the water, water as extractant the crude methanol into dimethyl ether and other compound contained in the separate light components, thus pre-column based products mainly light components such as dimethyl ether, and the tower bottom product mainly a mixture of methanol and water. Pre-column conditions are generally operated under normal pressure, the top temperature of 65. 75 or so, bottom of the column temperature is about 80 . Pre-tower trays usually installed 45.60, can achieve a theoretical separation step 25-35. Since the tower was extracted by methanol and water tower to tower bottom, so crude methanol feed opening position is relatively high, generally up from the bottom of the column number of the first 36-40 block board feed.Pre-Tata bottom outflow of methanol and water mixture immediately into the main tower, in the main tower of methanol and fusel achieve water separation. Usually installed in the main tower block tray 65-85, needs 36,050 a theoretical series (as the back flow of size). Many plant products are often stressed the tower of methanol concentration, while the outflow of water on the bottom of the column with methanol content less importance, so the pre-column to a mixture of methanol and water are in the lower half into the tower main tower. Location of the feed used by several bottom of the column 20 about a 26 plate. The main methanol distillation tower generally operate at atmospheric pressure. Tower operating temperature of 65-66 , bottom of the column operating temperature of 105 1IO. C. Tower refined methanol product generally require moisture 0.1%, methanol content 99.5%, while the bottom of the column with methanol content in the discharged water must be 0.5%. To prevent pre-tower with a light component to the main tower and moved with methanol on top of the tower was purified methanol product out of towers, the main tower from the top, generally in the first 10 or so side draw tray purified methanol product. High energy consumption of such processes, I plant steam consumption per ton of methanol in 2.1. 2.5t2 Transformation of methanol distillation line The transformation of methanol distillation system, can be used two ways: First, high efficient distillation column internals to improve the separation efficiency, reduce back flow, thereby reducing energy consumption; Another way is to change the separation line, and reduce energy consumption. Efficient use of methanol distillation tower internals can improve yield and reduce energy consumption with the role, but the magnitude does not meet expectations. At the same time changing the distillation process route to the greater effect of reducing energy consumption. The most commonly used pieces of high-Distillation Column with structured packing and efficient main tray two categories. According to the actual situation in our factory, structured packing does not apply to our plant expansion transformation of methanol distillation. Reasons are as follows.(1) The high separation efficiency of structured packing is mainly expressed in the hydrocarbon class system. For this type of material system, the liquids surface tension is very low, easy-to-the structured packing has a large number of surface area on the stretch, resulting in significant gas-liquid interfacial surface area, to achieve excellent separation efficiency. In the methanol distillation system is completely different. The liquid in the two towers contain a lot of water, so much higher than the surface tension of liquid organic hydrocarbon class. Thus the liquid surface in the filler dispersion is severely reduced, gas-liquid mass transfer efficiency is bound to fall significantly. Such as methanol distillation tower in the second half, close to 100% water content, surface tension is also close to 56dyn/cm (0.056N / m), as used in this condition, the structured packing, the separation is not satisfactory . I plant 3 104t / a methanol distillation device be transformed into an 8 104t / a methanol production capacity, regulatory (2) structured packing bed, the bed floor to the top always install the appropriate liquid distributor, so that downward flow of liquid to achieve uniform distribution along the tower section. However, the gradual downward flow of liquid, the initially uniform distribution along the tower section of the liquid will gradually accumulate to the tower wall. This phenomenon is known as wall flow (wall flow). When the wall of flow occurs, most of the liquid along the column wall to the downstream region, while most of the gas in the central region of upward flow tower. This has resulted in the separation of gas-liquid flow. Greatly reduced the contact between gas and liquid. One can imagine that at this time The structured packing distillation column can not have a good separation efficiency. To overcome this problem, generally when in the design of structured packing distillation column, a packed bed is only 6 seek to achieve a series of 10 theory, if a theory of distillation process requires far more than the number of series, they should be structured packing bed is divided into several sections, each distributor installed between the liquid and then to achieve uniform distribution of liquid flow again. However, this arrangement would allow the complex structure of the distillation column, expensive. By this analysis, using structured packing factory methanol distillation column transformation is not feasible. Can I use the highly efficient transformation of plant trays to methanol distillation column, in order to significantly reduce the energy consumption of methanol distillation system do? A variety of analysis shows that this approach to improve the system capacity, product purity methanol and methanol yield The effect is obvious, but the effect on reducing energy consumption, but also not very satisfactory. Distillation Technology Co., Ltd. Nanjing Canning production efficiency of composite hole miniature valve trays, is currently the only company approved by the U.S. research company distillation efficient industrial scale pilot test trays, the tower is equipped with a composite hole-board micro-valve, triangle to promote and multiple bubble hem downcomer, see Figure 2. With high flux, high separation efficiency, operating flexibility and so on. The tray efficiency than conventional tray more than 25%, using the plate transformation of factory pre-towers and methanol distillation tower, the original diameter of column under the conditions of constant expansion to meet the 8 104t / a methanol demand investment than the 50% reduction in use of structured packing, and can reduce the pre-tower water and back flow of the main tower. Which can reduce the energy consumption of methanol distillation system purposes. But the process simulation analysis shows that under these conditions methanol distillation system, lowering energy consumption is only about 5%, this rate is still relatively small, I still can not meet the methanol plant to expand output without increasing coal-fired boiler requirements. 2Canning affected companies around the three-dimensional map tray efficiency significantly reduce energy consumption from the point of view, only the replacement of high efficiency internals of this line is not enough, so it must be from the distillation point to find a better solution to the problem Methods.3 3 Tati can significantly reduce the energy consumption of pure alcoholIn many distillation system, people tend to unity of the two or three towers and two towers, and strive to reduce energy consumption. This means reducing energy consumption of machines is to reduce the number of evaporation and condensation of materials to reduce energy consumption. However, for methanol distillation, the people are the opposite of a tower will be divided into two towers, but they can make a lot of lower energy consumption. Addressed before the methanol distillation tower is a pre-extractive distillation. In the top of the tower by adding extractant - water, methanol and dimethyl ether and other light components separately. The towers energy consumption depends on water and feed composition, feed composition is a synthetic process (catalyst type. Synthesis of pressure, etc.) decisions, distillation section in not at liberty to demand for changes. The water is determined by methanol - dimethyl ether - water vapor-liquid equilibrium of three substances. Tower operating at atmospheric pressure as long as the pre-conditions, the vapor-liquid equilibrium is basically fixed, basically the size of water is fixed. Thus, the methanol distillation column at atmospheric pressure conditions expected little to change the process conditions to reduce energy consumption possibilities. Only by adopting high efficiency plate, increase the separation efficiency, reduce return flows to reduce energy consumption. However, the methanol distillation tower distillation process is not the case. Methanol distillation tower tower feed from the bottom of pre-mixture of methanol and water. In the methanol distillation tower for the separation process is actually heating of methanol evaporation from the water out of the process. In the process of distillation towers, the main tower of the role of distillation tower bottom is put in enough calories to make methanol out of the water completely evaporated, condensing in the top of the tower be refined methanol product. German Lurgi Company in the development of its low pressure methanol synthesis process, the use of the three columns of methanol purification process. This process will be methanol distillation tower is divided into two towers: the Pressurized and atmospheric distillation column distillation. The process shown in Figure 3.2、譯文甲醇精餾采用高效塔板和工藝路線的改進(jìn)摘要 簡要說明了甲醇精餾塔的內(nèi)件改造方案：復(fù)合孔微型闊高效塔板，比規(guī)整填料更適宜、更優(yōu)越；分析了甲醇精餾三塔工藝比雙塔工藝的優(yōu)越性和經(jīng)濟(jì)效益。關(guān)鍵詞 高效塔板 工藝路線 改進(jìn)對許多化工單元來說，能耗總是其技術(shù)經(jīng)濟(jì)指標(biāo)的一個重要因素。節(jié)約能源，降低消耗，加快技改步伐，實(shí)施產(chǎn)品結(jié)構(gòu)調(diào)整，是每個企業(yè)爭生存、求發(fā)展的重要措施?，F(xiàn)就我廠技改后甲醇精餾闡述采用高效塔板和改進(jìn)工藝路線，對降低能耗起到的重要作用。生產(chǎn)實(shí)踐證明，對于甲醇精餾分離，不能僅依靠高效塔內(nèi)件應(yīng)用于精餾塔中，以達(dá)到明顯地降低甲醇精餾能耗，而甲醇精餾工藝流程的改進(jìn)也可以使該系統(tǒng)的能耗明顯下降。1 甲醇精餾雙塔流程目前，大部分甲醇精餾過程均采用雙塔分離流程。我廠現(xiàn)有一套3104ta甲醇雙塔精餾裝置，2002年12月擬擴(kuò)建為8104ta甲醇雙塔精餾裝置，其流程見圖1。這一流程主要由兩個精餾塔構(gòu)成：預(yù)塔和主塔。由甲醇合成工段來的粗甲醇含甲醇86左右，首先進(jìn)入預(yù)塔，預(yù)塔實(shí)際上是一個萃取精餾塔，在塔頂加入相當(dāng)于粗甲醇進(jìn)料20。30左右的水，以水為萃取劑將粗甲醇進(jìn)料中所含的二甲醚等輕組份分開，因而預(yù)塔塔頂產(chǎn)品主要是二甲醚等輕組分，而塔底產(chǎn)品中則主要是甲醇與水的混合物。預(yù)塔一般都在常壓條件下操作，塔頂溫度為65。75左右，塔底溫度為80左右。預(yù)塔內(nèi)一般安裝有4560塊塔板，能達(dá)到2535個理論分離級數(shù)。由于該塔是通過塔頂加水萃取甲醇至塔底，故粗甲醇進(jìn)料口位置比較高，一般在由塔底向上數(shù)第3640塊板上進(jìn)料。預(yù)塔塔底流出的甲醇與水的混合物立即進(jìn)入主塔，在主塔內(nèi)實(shí)現(xiàn)甲醇與雜醇、水的分離。主塔一般安裝有6585塊塔板，需要36 0 50個理論級數(shù)(視回流量大小而定)。許多生產(chǎn)裝置往往強(qiáng)調(diào)塔頂甲醇產(chǎn)品濃度，而對塔底流出水中的甲醇含量不太重視，所以由預(yù)塔來的甲醇與水的混合物往往在主塔下半部分入塔。常用的進(jìn)料位置在由塔底數(shù)起第20一26塊塔板左右。甲醇精餾的主塔一般均在常壓下操作。塔頂操作溫度為6566，塔底操作溫度為1051IO。C。塔頂?shù)木状籍a(chǎn)品一般要求含水量01，甲醇含量995，而塔底排放水中的甲醇含量必須05。為防止預(yù)塔中輕組份帶至主塔并隨甲醇上移至塔頂而被精甲醇產(chǎn)品帶出塔，主塔一般均在距塔頂?shù)?0塊塔板左右側(cè)線采出精甲醇產(chǎn)品。此種流程能耗較高，我廠每噸甲醇耗蒸汽在21。25t。2甲醇精餾改造路線探討甲醇精餾系統(tǒng)的改造可以采用兩種方法：一是采用高效精餾塔內(nèi)件來提高分離效率，降低回流量，從而降低能耗；另一種方法則是改變分離路線，以降低能耗。采用高效精餾塔內(nèi)件可提高甲醇收率兼具有降低能耗的作用，但其幅度不能滿足人們的期望。同時改變精餾工藝路線對降低能耗有更大的效果。目前常用的高效精餾塔內(nèi)件主要有規(guī)整填料和高效塔板兩大類。根據(jù)我廠實(shí)際情況，規(guī)整填料不適用于我廠甲醇精餾擴(kuò)產(chǎn)改造。原因分析如下。(1)規(guī)整填料的高分離效率主要是表現(xiàn)在輕烴類系統(tǒng)中。對于這一類物料系統(tǒng)來說，液相的表面張力極低，易于在規(guī)整填料所具有的大量表面積上舒展開，從而造成極大的氣液接觸表面積，達(dá)到極佳的分離效率。而在甲醇精餾系統(tǒng)中則完全不一樣。兩塔的液相中均含有大量的水份，使得液相表面張力大大高于輕烴類有機(jī)物。因而液體在填料表面上的分散能力大大下降，氣液傳質(zhì)效率也必然大幅度下降。如在甲醇精餾主塔的下半段，含水量接近100，表面張力也趨近于56dyncm(0056Nm)，如在此條件下采用規(guī)整填料，則分離效果并不理想。在我廠3104ta甲醇精餾裝置上改造成為8104ta甲醇生產(chǎn)能力，規(guī)整填料很難完成此項(xiàng)任務(wù)。(2)在規(guī)整填料床層中，床層最上方總要安裝適當(dāng)?shù)囊后w分布器，以使向下流動的液體達(dá)到沿塔截面均勻分布。然而在液體逐漸向下流動時，起先沿塔截面均勻分布的液體會逐漸地向塔壁積累。這種現(xiàn)象稱為“壁流”(wall flow)。當(dāng)壁流發(fā)生時，大部分液體沿塔壁區(qū)域向下流，而大部分氣體則在塔中心區(qū)域向上流。這就造成了氣液流動的分離。從而大大削弱了氣液之間的接觸?？上攵藭r的規(guī)整填料精餾塔不可能有很好的分離效率。為克服此問題，一般在設(shè)計規(guī)整填料精餾塔時，一段填料床層僅力求達(dá)到6一10個理論級數(shù)，如一精餾過程需要的理論級數(shù)遠(yuǎn)遠(yuǎn)超過此數(shù)，則應(yīng)將規(guī)整填料床層分為若干段，每段之間安裝液體再分布器，使液體流動再次達(dá)到均勻分布。但這種安排將使整個精餾塔的結(jié)構(gòu)復(fù)雜，造價昂貴。通過以上分析，采用規(guī)整填料改造我廠甲醇精餾塔是不可行的。是否可以用高效塔板來改造我廠甲醇精餾塔，以大幅度降低甲醇精餾系統(tǒng)的能耗呢?各種分析表明，這一途徑對提高系統(tǒng)處理能力、甲醇產(chǎn)品的純度和甲醇收率的效果明顯，但在降低能耗上的效果，還不能令人十分滿意。南京凱寧精餾技術(shù)有限公司生產(chǎn)的復(fù)合孔微型閥高效塔板，是目前國內(nèi)唯一一家經(jīng)美國精餾研究公司工業(yè)規(guī)模試驗(yàn)測試的高效塔板，該塔板上裝有復(fù)合孔微型閥、三角形鼓泡促進(jìn)器和多折邊降液管，見圖2。具有通量高，分離效率高，操作彈性大等特點(diǎn)。該塔板比常規(guī)塔板效率高25以上，采用此塔板改造我廠甲醇精餾預(yù)塔和主塔，在原塔徑不變的條件下能夠滿足擴(kuò)產(chǎn)8104ta甲醇的要求，投資比采用規(guī)整填料降低50，并且能夠降低預(yù)塔用水量和主塔回流量。從而達(dá)到降低甲醇精餾系統(tǒng)能耗之目的。但工藝模擬分析表明，在這種條件下甲醇精餾系統(tǒng)能耗的降低也只不過是5左右，這一幅度還是比較小的，仍然不能適應(yīng)我廠擴(kuò)大甲醇產(chǎn)量，而不增加燃煤鍋爐的要求。圍2凱寧公司商效塔板的立體圖從大幅度降低能耗的角度考慮，僅更換高效塔內(nèi)件這一路線還是不夠的，所以還必須從精餾工藝的角度去尋找解決問題的更好方法。3三塔提純甲醇可大幅降低能耗在許多精餾系統(tǒng)中，人們往往將兩塔合一或三塔并二，力求達(dá)到能耗的降低。這一途徑降低能耗的機(jī)在于減少物料蒸發(fā)與冷凝的次數(shù)，以減少能量消耗。然而，對于甲醇精餾提純來說，人們反其道而行之，將一塔分為二塔，卻可以使能耗大量的降低。前已述及，甲醇精餾的預(yù)塔是一萃取蒸餾塔。通過在塔頂加入萃取劑水，將甲醇與二甲醚等輕組份分開。該塔的能耗主要取決于用水量和進(jìn)料組成，進(jìn)料組成是由合成工藝(催化劑類型。合成壓力等)決定的，精餾工段不能隨意要求改變。而用水量則是取決于甲醇二甲醚水三種物質(zhì)的氣液平衡。只要預(yù)塔操作在常壓條件下，這一氣液平衡也是基本固定的，用水量的大小也基本被固定下來。因而，甲醇精餾預(yù)塔在常壓條件下幾乎沒有改變工藝條件以降低能耗的可能性。只有采高效塔板，提高分離效率，減少回流量來降低能耗。然而，甲醇精餾主塔內(nèi)的精餾過程卻不是這樣。甲醇精餾主塔的進(jìn)料是來自預(yù)塔底部甲醇與水的混合物。在甲醇精餾主塔內(nèi)進(jìn)行的分離過程實(shí)際上是在加熱條件下，甲醇從水中蒸發(fā)出來的過程。在雙塔精餾過程中，精餾主塔內(nèi)的作用就是在塔底施加足夠的熱量，使甲醇從水中完全蒸發(fā)出來，而在塔頂冷凝得到精甲醇產(chǎn)品。德國Lurgi公司在開發(fā)其低壓合成甲醇的工藝時，采用了三塔精餾甲醇提純流程。這一流程將甲醇精餾主塔分為兩個塔：加壓精餾塔和常壓精餾塔。其工藝流程圖見圖3。從甲醇預(yù)精餾塔底部出來的甲醇與水的混合物先進(jìn)入加壓精餾塔，在此塔頂部采出約占總產(chǎn)量50的精甲醇。加壓精餾塔底部物料必然濃度稍低的甲醇與水的混合物，該混合物再進(jìn)入常壓精餾塔進(jìn)一步將剩余甲醇與水分開。這一流程的設(shè)計和操作的關(guān)鍵在于適當(dāng)確定加壓塔的操作壓力，從而使得加壓塔塔頂蒸出的精甲醇?xì)鉃槌核自俜衅鞯臒嵩?，使得整個甲醇與水分離過程只需要在加壓塔底部從外部輸入熱量，而在常壓塔底部不需要從外部引進(jìn)熱量。從設(shè)備的角度上看，加壓塔塔頂?shù)睦淠骷礊槌核椎脑俜衅?。工藝分析表明，將甲醇精餾主塔一分為二，確實(shí)是可以節(jié)省相當(dāng)?shù)哪芰肯?。首先，對于常壓精餾塔其塔底溫度在105110。C左右。要使得加壓塔塔頂?shù)木状細(xì)獬蔀槌核自俜衅鞯臒嵩矗訅核敎囟葢?yīng)在120左右，塔頂壓力約056MPa(G)，考慮到加壓塔內(nèi)精餾塔板所造成的壓降，加壓塔底部壓力應(yīng)為06MPa(G)左右，而塔底溫度只有130左右。為對這種溫度下的甲醇液體加熱氣化，使用一般的低壓蒸汽即可。換句話說，三塔流程加壓塔再沸器所需蒸汽和雙塔流程常壓塔再沸器所需蒸汽基本上是同等級的。其二，在采用三塔流程后，加壓塔和常壓塔頂分別采出約50的精甲醇。而這兩塔回流比基本相同，因而，這兩個塔內(nèi)的蒸發(fā)量基本相同，從而塔底部再沸器所需的熱量也相同。由于三塔流程中加壓塔和常壓塔的甲醇蒸發(fā)總量以及兩塔的回流量之和均與雙塔流程中精餾主塔基本一樣，故三塔流程中加壓塔和常壓塔內(nèi)蒸發(fā)量之和以及塔底吸收熱量均應(yīng)與雙塔流程中精餾主塔一樣。但由于三塔流程中僅僅加壓塔需圈三塔精餾甲醇提純藏程要從外部吸收熱量實(shí)現(xiàn)塔內(nèi)的氣化，故三塔流程所需外部供給的熱量必定少予雙塔流程所需外部供給的熱量。由此可以看出，三塔流程中加壓塔所需能耗僅為雙塔流程中常壓精餾主塔能耗的53，即在甲醇與水分離這一步，能量消耗下降了47。而對整個甲醇精餾系統(tǒng)(包括甲醇精餾預(yù)塔)來說。三塔流程的能耗比雙塔流程要少30左右。4應(yīng)用效果我廠原3104ta甲醇精餾裝置，為雙塔工藝。預(yù)塔塔徑1400，主塔塔徑1800，在2003年8104ta甲醇擴(kuò)產(chǎn)技改過程中，為節(jié)約投資，充分利用原有設(shè)備，選用了南京凱寧精餾技術(shù)有限公司生產(chǎn)的復(fù)合孔微型閥高效塔板，在塔徑、塔高不變的情況下，改造預(yù)塔，滿足了提產(chǎn)160的要求。利用舊飽和熱水塔新建一直徑01 800的加壓精餾塔，同樣選用復(fù)合孔微型閥高效塔板，以保證足夠的通量和分離效果。同時由雙塔改造為三塔提純甲醇工藝流程。該工程于2003年4月完成，開車至今甲醇精餾系統(tǒng)產(chǎn)品產(chǎn)量、產(chǎn)品純度、甲醇收率等各項(xiàng)指標(biāo)均達(dá)到或超過設(shè)計要求，特別是甲醇質(zhì)量，能與進(jìn)口甲醇媲美，受到上海各大用戶好評。單位甲醇能耗得到了較大幅度地下降，取得了令人滿意的效果。5經(jīng)濟(jì)效益分析(1)由于我廠采用的是高壓法生產(chǎn)甲醇，所以粗甲醇中雜質(zhì)含量較高，給甲醇精餾提純帶來了一定難度，原3104ta甲醇精餾系統(tǒng)日處理lOOt精甲醇已達(dá)到了滿負(fù)荷或超負(fù)荷運(yùn)行。也就是說，若利用原有技術(shù)，采用普通塔板，擴(kuò)產(chǎn)8104ta甲醇，需新增一套5104ta甲醇精餾裝置，同時還需新增一臺lOth燃煤鍋爐。需增加投資700多萬元。采用高效塔板和三塔精餾工藝只需投資110萬元就完成了8104ta甲醇精餾裝置的改造，節(jié)約投資600萬元左右。(2)由于采用了高效塔板，預(yù)塔內(nèi)不再加水，噸醇可節(jié)約軟水230kg左右，按10元t水計，年可節(jié)約023080 00010=184(萬元)(3)主、預(yù)塔回流量較原裝置單位產(chǎn)品下降3 9663 5268=4932kgt甲醇。由于甲醇精餾耗電與其他車間沒有分開，只能從泵配用的總功率(3104ta醇總功率為43kw，8104ta甲醇新工藝總功率為83kw)上與原裝置相比，在單位產(chǎn)品上有較大降低。(4)蒸汽消耗由原來的2125tt甲醇下降為12。14tt甲醇，按60t汽計，年可節(jié)省180 000 x 60=480(萬元)，基本上實(shí)現(xiàn)了擴(kuò)大甲醇產(chǎn)量而不增加燃煤鍋爐的要求。(5)由于加壓塔回流液不需用冷卻水冷卻，雖然擴(kuò)大了甲醇產(chǎn)量，循環(huán)冷卻水用量增加不多，仍采用原3104ta甲醇循環(huán)冷卻水裝置，滿足了8104ta甲醇精餾提純要求，節(jié)約了冷卻水及冷卻水電耗。6結(jié)束語盡管三塔提純甲醇流程已經(jīng)是很成熟的技術(shù)了，但目前國內(nèi)僅有少數(shù)幾家采用。而新型復(fù)合孔微型閥高效塔板在甲醇精餾裝置中我廠是國內(nèi)首家采用，因而這一先進(jìn)工藝技術(shù)和高效塔板還需進(jìn)一步推廣。參考文獻(xiàn)(1) 魏文德有機(jī)化工原料大全第二版北京：化學(xué)工業(yè)出版社，1999。804822(2) 謝克昌，李忠甲醇及其衍生物北京：化學(xué)工業(yè)出版社，2002(3) 吉林化學(xué)工業(yè)公司化肥廠二氧化碳參加合成甲醇反應(yīng)試驗(yàn)石油化工設(shè)計1977(2)：9。16(4) 化學(xué)工業(yè)出版社化工生產(chǎn)流程圖解北京：化學(xué)工業(yè)出版社，1990，3237(5) 王樹楹現(xiàn)代填料技術(shù)指南北京：中國石化出版社，1998，84(6) Henry ZKistarDistillation OperationNew York：McGrawHillInc7176甲醇精餾采用高效塔板和工藝路線的改進(jìn)