TWI765079B - Method for treating crude oil tank bottom sludge - Google Patents
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Abstract
一種用於處理原油槽底泥的方法，包含一油泥預處理步驟，一旋流三相分離步驟、一石油氣氧化焚燬步驟、一液態觸媒萃取步驟、一液態觸媒回收步驟，其中於該旋流三相分離步驟所產生的油品回收至回收油暫存槽以便後送至原油槽供銷售，廢氣則導入該石油氣氧化焚燬步驟進行氧化焚燬，於該液態觸媒萃取步驟所產生之固體廢棄物則可直接掩埋或加以固化再利用；於該液態觸媒萃取步驟所產出之原油及液態觸媒混合物則先送入混合液暫存槽，等待送入後段之液態觸媒回收步驟將液態觸媒回收循環再利用。 A method for treating crude oil tank bottom sludge, comprising a sludge pretreatment step, a cyclone three-phase separation step, a petroleum gas oxidative incineration step, a liquid catalyst extraction step, and a liquid catalyst recovery step, wherein in the The oil produced in the cyclone three-phase separation step is recovered to the recovered oil temporary storage tank for later delivery to the crude oil tank for sale, and the waste gas is introduced into the LPG oxidative incineration step for oxidative incineration. Solid waste can be directly buried or solidified and reused; the crude oil and liquid catalyst mixture produced in the liquid catalyst extraction step are first sent to the mixed liquid temporary storage tank, waiting to be sent to the subsequent liquid catalyst recovery step The liquid catalyst is recycled and reused.
Description
本發明係有關於一種處理原油槽底泥的方法，特別是指其為一種處理經由原油槽清理作業而移出油槽外的油泥的方法。 The present invention relates to a method for treating bottom sludge of crude oil tank, in particular, it refers to a method for treating sludge removed from oil tank through crude oil tank cleaning operation.
基於安全考量，依據工業安全要求，用於儲存原油之儲槽必須至少每隔五年開槽乙次進行安全檢查，而為了能仔細檢查及確認油槽結構、管件、槽底、排水設施、油槽壁、以及其它主要架構均仍然完好可用，通常業主都會將原油槽中存放的原油先行抽離，再將油槽底部的油泥清除出油槽外，再以蒸汽或高溫熱水對油槽內部的油槽壁以及底板進行清洗，直至檢查人員可進入槽內用肉眼對整個油槽進行詳細檢查為止。 Based on safety considerations, according to industrial safety requirements, the storage tanks used to store crude oil must be slotted for safety inspection at least once every five years. , and other main structures are still intact and available. Usually, the owner will first extract the crude oil stored in the crude oil tank, and then remove the sludge at the bottom of the oil tank out of the oil tank, and then use steam or high-temperature hot water to the oil tank wall and bottom plate inside the oil tank. Cleaning is carried out until the inspector can enter the tank to conduct a detailed inspection of the entire oil tank with the naked eye.
而經移除至油槽外的原油槽底泥，為能減少其體積以便進一步處理，一般做法是要求承包商使用離心分離機(Decanter)或其它設備對油泥進行「減積」處理，以離心力將油泥中的固體物與原油分離，以便進行後續處理；之後，經離心分離回收的原油則以油罐車載運送回其它原油槽與原油混合，而殘餘的固體物(Dry Cake)，則被裝入50加侖鐵桶內，運送至焚化廠攙配入燃煤中一起焚燒，既能增加燃煤熱值，又可將這些殘餘固體物澈底銷燬，因此，此種方法乃市面上所通行的工法。 In order to reduce the volume of the crude oil tank bottom sludge removed from the oil tank for further processing, the general practice is to require the contractor to use a centrifugal separator (Decanter) or other equipment to "de-accumulate" the sludge. The solids in the sludge are separated from the crude oil for subsequent processing; after that, the crude oil recovered by centrifugation is transported back to other crude oil tanks to be mixed with the crude oil, and the residual solids (Dry Cake) are put into In a 50-gallon iron drum, it is transported to an incineration plant and mixed with coal for incineration, which can not only increase the calorific value of the coal, but also completely destroy these residual solids. Therefore, this method is a common method in the market.
然而，由於原油槽底泥於處理前所含之油份高達百分之九十以上(90%)，其主要成份則是瀝青質及石蠟，因其黏滯性很強，因此能夠牢 固的附著在油泥中的固體廢棄物表面及洞孔內(Porous)，以Decanter所產生的離心力，跟本無法將之與固體物分離，因此，依據實測數據，如以體積(volume V%)做為測試基準時，經過離心分離機所處理過後裝桶的油泥，其固體物所含比例約為百分之十五(15%)，而濕度(Moisture)即液狀物含油及水則約為百分之八十五(85%)，而在液狀物中其中約有百分之五十(50%)是油份即碳氫化合物，其餘的液態物質35%則是水份。如果以重量(weight wt%)做為測量基準時，由於固體廢棄物比重可高達2.7(2.7g/kg)，而碳氫化合物的比重則約在0.9(0.9g/kg)，因此，如以固體物重量為測量基準(wt%)，則殘留在固體廢棄物表面及洞孔中的碳氫化合物其含量仍高達5%以上，而含水量則在3~5%之間。 However, since the crude oil tank bottom sludge contains more than 90% (90%) oil before treatment, its main components are asphaltenes and paraffins, which are highly viscous and therefore can be firmly attached On the surface of solid waste and in the pores (Porous) in the sludge, the centrifugal force generated by Decanter cannot separate it from the solid. Therefore, according to the measured data, such as volume (volume V%) as the test At the benchmark, the sludge that has been processed by the centrifuge and then filled into barrels contains about fifteen percent (15%) of solids, while the moisture (Moisture), that is, liquids containing oil and water, is about 10%. Eighty-five percent (85%) of the liquid, and about fifty percent (50%) of the liquid is oil, that is, hydrocarbons, and 35% of the rest of the liquid is water. If the weight (weight wt%) is used as the measurement benchmark, since the specific gravity of solid waste can be as high as 2.7 (2.7g/kg), and the specific gravity of hydrocarbons is about 0.9 (0.9g/kg), therefore, if using If the weight of solids is the measurement basis (wt%), the content of hydrocarbons remaining on the surface and holes of solid waste is still as high as 5% or more, while the water content is between 3 and 5%.
就以上的資料可知，經由離心分離處理而裝載於50加侖鐵桶內待進一步處理的油泥其所含的的碳氫化合物高達其體積比高達50%以上，以一只有效容積10萬公秉的原油槽為例，每5年中所產生的槽底油泥約有2,000公秉，以離心機對此油泥進行減積，則固體廢棄物及固形物之體積仍有200公秉之譜，而此200公秉的固體廢棄物中所含之原油則仍高達100公秉；如以原油之比重為900kg/M3為準，則以重量計的原油則有90公噸(90MT)，或者是近500桶的原油(500bbls)；如此大量的原油以焚化方式焚燬所造成的資源浪費不言可喻，而其因焚燒所產生的空氣污染排放物對環境所造成的衝擊更不待言。 From the above information, it can be seen that the oil sludge loaded into the 50-gallon iron drum for further treatment after centrifugal separation contains hydrocarbons as high as 50% of its volume ratio. Take the crude oil tank as an example, the sludge at the bottom of the tank is about 2,000 hectares generated every 5 years. If the sludge is reduced by a centrifuge, the volume of solid waste and solids is still 200 hectares. The crude oil contained in the solid waste of 200 kilograms is still as high as 100 kilograms; if the specific gravity of crude oil is 900kg/M3, the crude oil by weight is 90 metric tons (90MT), or nearly 500 barrels of crude oil (500bbls); the waste of resources caused by the incineration of such a large amount of crude oil is self-evident, and the impact on the environment caused by the air pollution emissions caused by incineration is not to mention.
雖然，市面上除了以離心分離機進行處理的工打之外，也有採用熱裂解(Pyrolysis)對油泥進行間接加熱的熱裂解工法；但由於採用熱裂解工法需於厭氧狀態下將物料加熱至550℃以上使油泥沸騰及蒸發，但由於 油泥中的水及油於此一溫度會有共沸問題，因此，所產出的廢水會含有高比例的含油量，而回收油中也有高比例的含水量，因此如要加以回收則必須進行再處理，或者在熱裂解塔的冷凝塔段增加幾個「再循環蒸餾」的構造，如此一來，控制裝置會變得很複雜，且作業成本大幅提高。另外，由於熱裂解需採用「批組式」(Batch Type)方式操作，製程效率不高則是另一個障礙，因此，直至目前，此一熱裂解工法於市場上並不常見。 Although, in addition to the process of processing with centrifugal separators, there are also thermal cracking processes that indirectly heat the sludge by thermal cracking (Pyrolysis); Above 550℃, the sludge boils and evaporates, but since the water and oil in the sludge will have azeotrope problems at this temperature, the produced wastewater will contain a high proportion of oil content, and the recovered oil also has a high proportion of oil. Therefore, if it is to be recovered, it must be reprocessed, or several structures of "recycle distillation" should be added to the condenser section of the thermal cracking tower. As a result, the control device will become very complicated, and the operating cost will be large. improve. In addition, since thermal cracking needs to be operated in a "Batch Type" method, low process efficiency is another obstacle. Therefore, until now, this thermal cracking method is not common in the market.
有如前述，由於原油槽底泥中逾90%都是原油成份，因此，無論以何種方工法對油泥進行處理，最終目標均需將油泥中的原油全數回收才是正途，除了可避免造成資源浪費之外，亦可避免焚燒油泥形成空氣污染對環境造成衝擊。 As mentioned above, since more than 90% of the sludge in the crude oil tank bottom is crude oil, no matter what method is used to treat the sludge, the ultimate goal is to recover all the crude oil in the sludge. In addition to waste, it can also avoid the impact on the environment caused by air pollution caused by burning sludge.
爰是，本發明人乃本著多年從事原油槽底泥之控制、減量、以及相關業務之實務經驗，積極潛心研發思考，再配合實際之實驗，致有本發明之產生。 The fact is, the inventor of the present invention is based on years of practical experience in the control, reduction and related business of crude oil tank bottom sludge, actively concentrates on research and development thinking, and cooperates with actual experiments, resulting in the invention of the present invention.
本發明係在提供一種處理原油槽底泥的方法，對於已清出油槽外之油泥，進行完整的處理；整個方法則包含有六個可獨立運作的步驟，茲分述如下：一油泥預處理步驟，係將油泥進行過濾以及均質化之預處理，方法是先將油泥中粗大的固形物例如大型石塊、螺斯、鐵片等等，先行濾除，且將油泥送入預熱槽先行預熱使油泥呈流動狀態，以利送入下一階段之處理步驟即該旋流三相分離步驟進行處理。 The present invention is to provide a method for treating the bottom sludge of crude oil tank, and complete treatment of the sludge outside the oil tank; the whole method includes six steps that can be operated independently, which are described as follows: 1. Pretreatment of sludge The first step is to filter and homogenize the sludge. The method is to first filter out the coarse solids in the sludge, such as large stones, screws, iron pieces, etc., and send the sludge into the preheating tank first. Preheating makes the sludge in a flowing state, so that it can be sent to the next processing step, that is, the cyclone three-phase separation step for processing.
一旋流三相分離步驟，係利用高溫蒸汽做為搓洗劑，於一旋 流三相分離機的旋流(Cyclone)槽內將油泥進行搓洗加熱使碳氫化合物溶解及懸浮、使廢水蒸發、以及石油氣揮發，進而令油、水、固體廢棄物及石油氣均被分離出來；一石油氣氧化焚燬步驟，係利用一熱氧化焚燬裝置(Thermal Oxidation Device)，將產自該旋流三相分離機的石油氣抽取、蒐集之後，再以熱氧化法(Thermal Oxidation)將其氧化及焚燬(Combustion)；一液態觸媒萃取步驟，係接續於該旋流三相分離步驟之後，於該旋流三相分離步驟將油與水分離後，針對所殘留的該固體廢棄物包含多孔隙(Porous)的結構物，黏滯性很高的碳氫化合物，應用一微氣泡萃取步驟配合液態觸媒，以衝激的方式，讓粒徑小至20Micron(0.02mm)的微氣泡攜帶液態觸媒滲入固體廢棄物的洞孔內，將殘留於多孔隙的固體廢棄物(Porous)表面及洞孔內的碳氫化合物即油份全部萃取出來；一廢水處理步驟，係接續於該旋流三相分離步驟，將產自該旋流三相分離機之廢水進行處理，該廢水處理步驟包含一精密油水分離步驟、一活性碳吸附步驟、一陰陽離子交換步驟，用以將廢水中所殘留的碳氫化合物全部去除，能將此一放流水回收再利用。 A cyclone three-phase separation step is to use high-temperature steam as a scrubbing agent to scrub and heat the sludge in a cyclone tank of a cyclone three-phase separator to dissolve and suspend hydrocarbons, evaporate waste water, and volatilization of the petroleum gas, so that oil, water, solid waste and petroleum gas are all separated; a petroleum gas oxidation incineration step uses a thermal oxidation incineration device (Thermal Oxidation Device), will produce the three-phase swirl flow After the LPG of the separator is extracted and collected, it is oxidized and combusted by Thermal Oxidation. A liquid catalyst extraction step is followed by the cyclone three-phase separation step. After the oil and water are separated in the three-phase separation step, a microbubble extraction step is applied to the residual solid waste containing porous structures and hydrocarbons with high viscosity. , in the way of impulse, let the micro-bubble with particle size as small as 20Micron (0.02mm) carry the liquid catalyst to penetrate into the holes of the solid waste, and will remain on the surface of the porous solid waste (Porous) and in the holes. The hydrocarbons, that is, the oil, are all extracted; a wastewater treatment step, which is followed by the cyclone three-phase separation step, treats the wastewater produced by the cyclone three-phase separator, and the wastewater treatment step includes a precision oil-water The separation step, an activated carbon adsorption step, and an anion and cation exchange step are used to remove all the hydrocarbons remaining in the waste water, and the effluent water can be recycled and reused.
較佳者，該旋流三相分離步驟係將油泥先送入一油泥攪拌槽中，並藉由135℃之蒸汽通過該油泥攪拌槽底部之蒸汽盤管對油泥間接加熱，之後，再將油泥輸送至旋流三相分離機主體裝置(Main Unit)之旋流槽體(Cyclone)中；而蒸汽則從反方向進入旋流槽對油泥產生衝撞及搓洗效應，使油泥中的油份往上懸浮，而於135℃溫度下已達揮發狀態的廢水則變成蒸汽往上揮發，經三相分離機上方之冷凝段之後，還原成液態水體流入廢水 暫存槽，再輸送至該廢水處理步驟進行廢水處理，而於此135℃工作溫度下已變成石油氣之C1H4~C3H8等碳氫化合物則變成氣體往上懸浮，再由外部真空泵對管線內部抽真空之效應，使石油氣被抽送經過一冷凝器冷凝，之後，再藉由真空罐下方被抽離，導入該石油氣氧化焚燬步驟氧化及焚燬。 Preferably, in the cyclone three-phase separation step, the sludge is firstly fed into a sludge stirring tank, and the sludge is indirectly heated by steam at 135° C. through the steam coil at the bottom of the sludge stirring tank, and then the sludge is heated. It is transported to the Cyclone of the Main Unit of the cyclone three-phase separator; while the steam enters the cyclone from the opposite direction to produce a collision and scrubbing effect on the sludge, so that the oil in the sludge goes up. Suspended, and the wastewater that has reached a volatilized state at a temperature of 135 °C turns into steam and volatilizes upward. After passing through the condensation section above the three-phase separator, it is reduced to liquid water and flows into the wastewater temporary storage tank, and then sent to the wastewater treatment step. Wastewater treatment, and the hydrocarbons such as C1H4~C3H8 that have turned into petroleum gas at the working temperature of 135 °C will become gas and suspend upward, and then the external vacuum pump will vacuum the inside of the pipeline, so that the petroleum gas is pumped through a condensation process. After that, the vacuum tank is evacuated from the bottom of the vacuum tank and introduced into the LPG oxidation and incineration step for oxidation and incineration.
較佳者，經過三相分離步驟處理之殘餘固體廢棄物則在該旋流三相分離機之旋流艙(Cyclone)底部持續堆積，直至固體廢棄物堆積至一定之總量時，該旋流三相分離機底部之閘刀閥開啟，殘留之固體廢棄物則落入下方之廢油渣暫存槽，以待送入該液態觸媒萃取步驟進行進一步處理；而經由該旋流三相分離機處理後所回收之油料則直接送入一回收油暫存槽，待該回收油暫存槽達到高液位狀態，再將油料送入原油儲槽。 Preferably, the residual solid waste processed by the three-phase separation step is continuously accumulated at the bottom of the cyclone chamber (Cyclone) of the cyclone three-phase separator, until the solid waste accumulates to a certain total amount, the cyclone will continue to accumulate. The gate knife valve at the bottom of the three-phase separator is opened, and the residual solid waste falls into the waste oil residue temporary storage tank below, to be sent to the liquid catalyst extraction step for further processing; and through the cyclone three-phase separation The oil recovered after the machine treatment is directly sent to a temporary storage tank for recovered oil. After the temporary storage tank for recovered oil reaches a high liquid level, the oil is sent to the crude oil storage tank.
較佳者，該石油氣氧化焚燬步驟係以密閉式氧化及焚燬裝置為核心，係將由該旋流三相分離步驟所分離出來的廢石油氣藉由一熱氧化焚毀裝置內建的抽氣裝置將石油氣導入一石油氣回收槽後，再藉由抽氣裝置抽送進入該熱氧化焚毀裝置之密閉式氧化槽中，經過氧化焚燬的廢氣則通過排氣控制裝置再排入大氣中。 Preferably, the LPG oxidation incineration step is based on a closed oxidation and incineration device, and the waste LPG separated by the cyclone three-phase separation step is passed through a thermal oxidation incineration device built-in air extraction device. After the LPG is introduced into a LPG recovery tank, it is pumped into the closed oxidation tank of the thermal oxidation incineration device through an air extraction device, and the exhaust gas after oxidation incineration is discharged into the atmosphere through an exhaust control device.
較佳者，該石油氣氧化焚燬步驟中，如果石油氣氧化時的溫度未達到氧化焚燬所設定的溫度，該熱氧化焚燬裝置所內建的進氣閥門開啟，將外部已配置的丙烷氣導入與廢石油氣混合一起氧化焚燬，以便所排出的氣體無任何廢石油氣。 Preferably, in the LPG oxidation incineration step, if the temperature of the LPG oxidation does not reach the temperature set by the oxidation incineration, the air inlet valve built in the thermal oxidation incineration device is opened, and the externally configured propane gas is introduced. It is oxidized and incinerated together with waste petroleum gas, so that the discharged gas does not contain any waste petroleum gas.
依照上述，可以避免石油氣儲存過久產生工安事故或環保議題。 According to the above, it is possible to avoid industrial safety accidents or environmental issues caused by long-term storage of LPG.
較佳者，該液態觸媒萃取步驟係將該旋流三相分離機所排出 的殘餘固體廢棄物輸送至一廢油渣暫存槽，再將殘餘固體廢棄物送入一氣泡式萃取機之萃取槽中，而之前，為設備初啟動之需已先投入液態觸媒於萃取槽中，再經過系統所設的微氣泡生裝置以及槽內預設置噴嘴所射出之微氣泡之振盪及清洗後，殘留在固體廢棄物表面及孔洞中的碳氫化合物包含瀝青質以及石蠟均會被溶解及清洗出來，而與液態觸媒形成混合物；之後，再繼續投入殘餘固體廢棄物時，再將原已儲存在一液態觸媒儲槽的液態觸媒依據所投入的殘餘固體物設定一重量百分比例，而將液態觸媒輸送入該微氣泡萃取機的清洗振盪槽；而由於持續投入物料即殘餘固體廢棄物及液態觸媒，因此，在最高液位以上的液態觸媒以及碳氫化合物的混合物則會持續升高而產生溢流現象再進入溢流液暫存槽，待液位持續升高達到高液位時，再將混合液輸送至回收油/液態觸媒混合物暫存槽，等到液位升高至高液位時，再輸送進入該液態觸媒回收步驟。 Preferably, in the liquid catalyst extraction step, the residual solid waste discharged from the cyclone three-phase separator is sent to a waste oil residue temporary storage tank, and then the residual solid waste is sent to a bubble extractor. In the extraction tank, before, for the initial start-up of the equipment, a liquid catalyst has been put into the extraction tank, and then the microbubble generated by the system and the pre-set nozzles in the tank are oscillated and cleaned. , the hydrocarbons including asphaltenes and paraffins remaining on the surface of the solid waste and in the pores will be dissolved and washed out to form a mixture with the liquid catalyst; The liquid catalyst stored in a liquid catalyst storage tank is set at a weight percentage according to the input residual solids, and the liquid catalyst is transported into the cleaning and shaking tank of the microbubble extractor; and because the continuous input of materials is the residual solids Waste and liquid catalyst, therefore, the mixture of liquid catalyst and hydrocarbon above the highest liquid level will continue to rise, resulting in overflow phenomenon and then enter the overflow liquid temporary storage tank, until the liquid level continues to rise to reach When the liquid level is high, the mixed liquid is transported to the temporary storage tank of the recovered oil/liquid catalyst mixture, and when the liquid level rises to the high liquid level, it is transported to the liquid catalyst recovery step.
依照上述，係將經過固/液分離後的殘留固體廢棄物以微氣泡萃取配合液態觸媒為萃取劑將殘留在固體廢棄物中的碳氫化合物完全取出，使得殘留之固體廢棄物不含任何碳氫化合物，可直接掩埋進行固化處理。 According to the above, the residual solid waste after solid/liquid separation is extracted with microbubble and the liquid catalyst is used as the extractant to completely remove the hydrocarbons remaining in the solid waste, so that the residual solid waste does not contain any Hydrocarbons, which can be directly buried for curing.
較佳者，該液態觸媒回收方法包含兩個以分子蒸餾器為核心之第一階段分子蒸餾步驟及第二階段分子蒸餾步驟，該第一階段分子蒸餾步驟係將液態觸媒及回收油混合物送經預熱器，經過加溫後再進入第一個分子蒸餾器，物料即液態觸媒及回收油的混合物旋即被第一個分子蒸餾器持續旋轉的刮板刮至汽缸壁形成一薄膜，而由於外部的真空泵持續透過冷井的管道對第一個分子蒸餾器內部持續抽真空，因此第一個分子蒸餾器的 內部保持一工作壓力，於該工作壓力下，形成薄膜黏附於第一個分子蒸餾器汽缸壁的混合液於分子自由程的效應下，部份已經達到沸點(Boling point)的分子亦即液態觸媒變成揮發性氣體，由於分子蒸餾器持續經由外部抽真空，因此，通往外部管道的壓力形成一個急速下降的壓差，而這些已經蒸發的液態觸媒分子(Molecular)即霧狀(Mist)液態觸媒則往壓力較低的管道出口移動，而移動至分子蒸餾器本體中央部位時，就被一組內置冷凝器阻擋，由於內置冷凝器的冷凝管表面溫度為略低於常溫之水溫，因此這些已經蒸發的液態觸媒分子與冷凝管道接觸後則立即被冷凝回復成液態，再循第一個分子蒸餾器下方的出口落入暫存槽，待高液位時再輸送回步驟之液態觸媒儲槽；沸點較高的回收油以及少量未能於第一分子蒸餾步驟被回收的液態觸媒混合液，則送至該第二階段分子蒸餾步驟中進行處理，以防因為液態觸媒於該第一階段分子蒸餾步驟中沒有被完全回收造成浪費；該第二階段之分子蒸餾步驟的配置及作業原理與該第一個分子蒸餾步驟相同。 Preferably, the liquid catalyst recovery method includes two first-stage molecular distillation steps and second-stage molecular distillation steps with a molecular distiller as the core, and the first-stage molecular distillation step is a mixture of liquid catalyst and recovered oil. It is sent to the preheater, and then enters the first molecular distiller after heating. The mixture of the material, the liquid catalyst and the recovered oil, is immediately scraped to the cylinder wall by the continuously rotating scraper of the first molecular distiller to form a thin film. Since the external vacuum pump continues to pump the vacuum inside the first molecular distiller through the pipeline of the cold well, the inside of the first molecular distiller maintains a working pressure, and under the working pressure, a film is formed to adhere to the first molecular distiller. Under the effect of molecular free path, the mixed liquid in the cylinder wall of the molecular distiller, some of the molecules that have reached the boiling point (Boling point), that is, the liquid catalyst, become volatile gas. The pressure to the external pipeline forms a rapidly decreasing pressure difference, and these vaporized liquid catalyst molecules (Molecular), that is, the mist (Mist) liquid catalyst, move to the outlet of the pipeline with lower pressure, and then move to the molecular distiller. When the central part of the main body is blocked by a set of built-in condensers, since the surface temperature of the condenser tube of the built-in condenser is slightly lower than the water temperature at room temperature, the evaporated liquid catalyst molecules will be condensed immediately after contacting the condensation tube. Return to liquid state, and then fall into the temporary storage tank through the outlet below the first molecular distiller. When the liquid level is high, it will be transported back to the liquid catalyst storage tank of the step. The liquid catalyst mixture recovered in the molecular distillation step is sent to the second-stage molecular distillation step for processing to prevent waste because the liquid catalyst is not completely recovered in the first-stage molecular distillation step; The configuration and operation principle of the two-stage molecular distillation step are the same as the first molecular distillation step.
依照上述，本步驟係用於將該液態觸媒回收步驟所產出之油料及液態觸媒之混合物中將液態觸媒回收，以供循環再利用。 According to the above, this step is used to recover the liquid catalyst from the mixture of oil and liquid catalyst produced in the liquid catalyst recovery step for recycling.
較佳者，該廢水處理步驟包含一精密油水分離機、一微過濾器、一陰陽離子交換器、一廢水暫存槽、一回收油暫存槽及二緩衝槽；由該旋流三相分離步驟所產出之廢水被輸送至該廢水暫存槽，待達到高液位之後抽送入精密油水分離機進行處理，經過處理後之廢水則被送入其中之一緩衝槽暫存，等到達到高液位後，再將廢水送入該微過濾器，以去除微小之油滴，之後廢水被導入另一緩衝槽暫存，等液位升高至高液位時，再 將廢水送入該陰陽離子交換槽做最終之處理。所謂陰陽離子乃使用經過選別的陰陽離子樹脂做為濾料，以吸附廢水中的的有害重金屬及礦物質，此一步驟則通稱為陰陽離子交換步驟。 Preferably, the wastewater treatment step includes a precision oil-water separator, a microfilter, an anion and cation exchanger, a wastewater temporary storage tank, a recovered oil temporary storage tank and two buffer tanks; the three-phase separation by the cyclone The waste water produced in the step is sent to the waste water temporary storage tank, and after reaching the high liquid level, it is pumped into the precision oil-water separator for treatment, and the treated waste water is sent to one of the buffer tanks for temporary storage until the high liquid level is reached. After the liquid level, the wastewater is sent to the micro filter to remove tiny oil droplets, and then the wastewater is introduced into another buffer tank for temporary storage. When the liquid level rises to a high liquid level, the wastewater is sent to the anion and cation The swap slot does the final processing. The so-called anions and cations use selected anion and cation resins as filter materials to adsorb harmful heavy metals and minerals in wastewater. This step is generally called an anion and cation exchange step.
依照上述，將產自該廢水處理步驟之廢水進行三階段的處理，包含精密油水分離步驟、微過濾步驟、以及陰陽離子交換步驟，以便所排放之廢水不含任何碳氫化何物，以便此一放流水可以回收再利用。 According to the above, the wastewater produced from the wastewater treatment step is treated in three stages, including a precision oil-water separation step, a microfiltration step, and an anion and cation exchange step, so that the discharged wastewater does not contain any hydrocarbons, so that this The drain water can be recycled and reused.
如上所述，針對目前市面上並無供應市場所需，可符合當今高環保標準的步驟能對原油槽底泥進行完整的處理，達成資源完全回收，且無造成任何二次污染的疑慮；因此，於目前，對於原油槽底泥多用採用兩相或三相離心分離機(Decanter Centrifuge)進行處理後再積存於油泥坑中(Oil Sludge Pit)等待進一步處理、就地掩埋(Landfill)，或以焚化方式焚燬；因此，其所將可能造成的二次污染勢無可避免。 As mentioned above, in view of the fact that there is currently no market demand, the steps that can meet today's high environmental protection standards can complete the treatment of crude oil tank bottom sludge, achieve complete resource recovery, and have no doubt of causing any secondary pollution; therefore; , At present, the bottom sludge of crude oil tank is mostly treated with a two-phase or three-phase centrifugal separator (Decanter Centrifuge) and then stored in the oil sludge pit (Oil Sludge Pit) for further treatment, in situ burial (Landfill), or with Incineration method is incinerated; therefore, the secondary pollution that it will cause is inevitable.
本發明的效益在於：製程標準化、操作方法簡單、作業成本相對較低、且最終所產出的固體廢棄物完全不再殘存任何的碳氫化合物，可直接進行掩埋或固化以供再利用；本發明方法及應用之裝置可供相關廠商運用，以便將原油槽底泥進行完整處理，達到資源完全回收且無任何二次污染的目標。 The advantages of the present invention lie in: standardized manufacturing process, simple operation method, relatively low operation cost, and no hydrocarbons remain in the solid waste finally produced, which can be directly buried or solidified for reuse; The inventive method and the applied device can be used by relevant manufacturers, so as to completely process the bottom sludge of the crude oil tank, so as to achieve the goal of complete resource recovery without any secondary pollution.
以下僅藉由具體實施例，且佐以圖式作詳細之說明，俾 貴審查委員能對於本發明之各項功能、特點，有更進一步之瞭解。 The following is only described in detail by specific embodiments and accompanying drawings, so that the examiners can have a further understanding of the various functions and characteristics of the present invention.
10‧‧‧油泥預處理步驟 10‧‧‧Sludge pretreatment steps
103‧‧‧油泥過濾篩 103‧‧‧Sludge filter
102‧‧‧物料輸送泵 102‧‧‧Material conveying pump
101‧‧‧凝析油儲存槽 101‧‧‧Condensate storage tank
104‧‧‧物料輸送泵 104‧‧‧Material transfer pump
105‧‧‧油泥預熱槽 105‧‧‧Sludge preheating tank
20‧‧‧旋流三相分離步驟 20‧‧‧Swirl three-phase separation steps
201‧‧‧油泥攪拌槽 201‧‧‧Sludge mixing tank
2011‧‧‧蒸汽盤管 2011‧‧‧Steam coil
202‧‧‧物料輸送泵 202‧‧‧Material conveying pump
203‧‧‧旋流三相分離機 203‧‧‧Swirl three-phase separator
204‧‧‧熱交換器 204‧‧‧Heat exchanger
205‧‧‧物料輸送泵 205‧‧‧Material transfer pump
207‧‧‧物料輸送泵 207‧‧‧Material transfer pump
208‧‧‧真空罐 208‧‧‧Vacuum Tank
209‧‧‧真空泵 209‧‧‧Vacuum Pump
210‧‧‧回收油暫存槽 210‧‧‧Temporary storage tank for recovered oil
211‧‧‧廢油渣暫存槽 211‧‧‧Temporary storage tank for waste oil residue
212‧‧‧冷凝器 212‧‧‧Condenser
30‧‧‧石油氣氧化焚燬步驟 30‧‧‧LPG Oxidative Incineration Steps
301‧‧‧石油氣回收槽 301‧‧‧LPG recovery tank
302‧‧‧熱氧化焚燬裝置 302‧‧‧Thermal oxidation incineration device
40‧‧‧液態觸媒萃取步驟 40‧‧‧Liquid catalyst extraction step
401‧‧‧微氣泡萃取機 401‧‧‧Microbubble Extractor
402‧‧‧廢油渣暫存槽 402‧‧‧Temporary storage tank for waste oil residue
403‧‧‧液態觸媒儲槽 403‧‧‧Liquid catalyst storage tank
404‧‧‧固體廢棄物儲桶 404‧‧‧Solid waste storage barrels
405‧‧‧回收油/液態觸媒混合物暫存槽 405‧‧‧Temporary storage tank for recovered oil/liquid catalyst mixture
406‧‧‧物料輸送泵 406‧‧‧Material transfer pump
407‧‧‧物料輸送泵 407‧‧‧Material transfer pump
408‧‧‧物料輸送泵 408‧‧‧Material transfer pump
41‧‧‧微氣泡萃取步驟 41‧‧‧Microbubble extraction steps
50‧‧‧液態觸媒回收步驟 50‧‧‧Liquid catalyst recovery steps
501‧‧‧分子蒸餾器 501‧‧‧Molecular Distiller
502:分子蒸餾器 502: Molecular Still
503:回收油儲槽 503: Recovery Oil Storage Tank
504:冰水系統 504: Ice water system
505:冷卻系統 505: Cooling system
506:中央加熱流體系統 506: Central Heating Fluid System
60:廢水處理步驟 60: Wastewater treatment steps
601:廢水暫存槽 601: Wastewater temporary storage tank
602:廢水進料輸送泵 602: Wastewater Feed Transfer Pump
603:回收油暫存槽 603: Recovered oil temporary storage tank
604:廢水進料輸送泵 604: Wastewater Feed Transfer Pump
605:精密油水分離機 605: Precision oil-water separator
606:緩衝槽 606: Buffer slot
607:廢水進料輸送泵 607: Wastewater Feed Transfer Pump
608:微過濾器 608: Micro Filter
609:緩衝槽 609: Buffer slot
610:廢水進料輸送泵 610: Wastewater Feed Transfer Pump
611:陰陽離子交換器 611: Anion and cation exchangers
第1圖 係本發明處理原油槽底泥的方法之方塊示意圖。 Fig. 1 is a block schematic diagram of the method of the present invention for treating the bottom sludge of crude oil tank.
第2圖 係本發明油泥預處理步驟之示意圖。 Fig. 2 is a schematic diagram of the sludge pretreatment steps of the present invention.
第3圖 係本發明旋流三相分離步驟之示意圖。 Figure 3 is a schematic diagram of the cyclone three-phase separation step of the present invention.
第4圖 係本發明石油氣氧化焚燬步驟之示意圖。 Figure 4 is a schematic diagram of the process of oxidative incineration of petroleum gas in the present invention.
第5圖 係本發明液態觸媒萃取步驟之示意圖。 Fig. 5 is a schematic diagram of the liquid catalyst extraction step of the present invention.
第6圖 係本發明液態觸媒回收步驟之示意圖。 Fig. 6 is a schematic diagram of the recovery step of the liquid catalyst of the present invention.
第7圖 係本發明廢水處理步驟之示意圖。 Fig. 7 is a schematic diagram of the wastewater treatment steps of the present invention.
請參閱第1圖，本發明處理原油槽底泥的方法包含一個油泥預處理步驟10，一旋流三相分離步驟20、一石油氣氧化焚燬步驟30、一液態觸媒萃取步驟40、一液態觸媒回收步驟50，以及應用相關裝置。下文將詳細說明之：該油泥預處理步驟10係將原油槽底油泥中大形的固體廢棄物先行移除，並將物理狀況不穩定的油泥做預處理，以便將經過預處理後的油泥送入後續之步驟20處理。 Please refer to FIG. 1, the method for treating crude oil tank bottom sludge according to the present invention includes a
該旋流三相分離步驟20利用高溫蒸汽做為搓洗劑，於一旋流三相分離機203的旋流(Cyclone)槽內將油泥進行搓洗加熱使碳氫化合物溶解及懸浮、使廢水蒸發、以及石油氣揮發，進而使油、水、固體廢棄物及石油氣均被分離出來。 The cyclone three-
該石油氣氧化焚燬步驟30則係利用一熱氧化焚燬裝置(Thermal Oxidation Device)302(參閱第4圖)，將產自該旋流三相分離機203的石油氣抽取、蒐集之後，再以熱氧化法(Thermal Oxidation)將其氧化及焚燬(Combustion)。 The LPG
該液態觸媒萃取步驟40係接續該旋流三相分離步驟20，於該旋流三相分離步驟20將油與水分離後，所殘留的該固體廢棄物包含多個多孔隙(Porous)的結構物，黏滯性很高的碳氫化合物，應用一微氣泡式萃取步驟41配合液態觸媒將多孔隙的固體廢棄物表面及洞孔中的碳氫化合物萃取出來。 The liquid
該液態觸媒回收步驟50包含有一組兩階段之分子蒸餾技術手段，以便將液態觸媒回收後，以供循環再利用供應給該液態觸媒萃取步驟40，並使分離回收的原油不含液態觸媒。 The liquid
請參閱第1圖，本發明處理原油槽底泥的步驟一實施例，該步驟更結合一廢水處理步驟60係接續該旋流三相分離步驟20，將產自旋流三相分離機203之廢水進行處理；該廢水處理步驟60包含一精密油水分離步驟、一活微過濾吸附步驟、一陰陽離子交換步驟，用以將廢水中所殘留的碳氫化合物全部去除，能將此一放流水回收再利用。 Please refer to FIG. 1, an embodiment of the step of the present invention for treating the bottom sludge of a crude oil tank. This step is further combined with a
請參閱第1圖、第2圖，該油泥預處理步驟10係將油泥進行預處理，可將較大體積之廢棄物惕除，使油泥呈液狀具良好的流動性，以便將油泥送入下一階段之步驟20進行處理。 Please refer to Fig. 1 and Fig. 2, the
油泥處理步驟係將待處理的油泥送入油泥過濾篩103，將油泥中體積過大的固形物移除，讓油泥的固體廢棄物粒徑保持在直徑約2~3mm之間，以利後續的步驟作業之需；經過油泥過濾篩103的油泥則經過物料輸送泵104送入油泥預熱槽105，經過預處理步驟之油泥則可導入後續作業步驟。 The oil sludge treatment step is to send the oil sludge to be treated into the oil
油泥預處理過程中，如部份油泥已呈固體狀，流動性不佳， 則於過程中可添加適量的凝析油或柴油，使步驟作業達到標準化的目標。 In the process of sludge pretreatment, if part of the sludge is solid and has poor fluidity, an appropriate amount of condensate or diesel oil can be added in the process to make the step operation reach the goal of standardization.
此一部份而可藉物料輸送泵102將儲存於凝析油儲存槽101的凝析油或柴油定量輸送到該粉過濾篩103之中，再進行攪拌使其均勻。 This part can be quantitatively transported to the
請參閱第1圖、第3圖，該旋流三相分離步驟20係將油泥先送入油泥攪拌槽201中，並藉由高溫較佳者例如135℃之蒸汽通過該油泥攪拌槽201底部之蒸汽盤管2011對油泥間接加熱，之後，再由物料輸送泵202輸送至旋流三相分離機203之主體裝置(Main Unit)之旋流(Cyclone)槽內中；而同一時間，蒸汽則從反方向進入旋流槽並對油泥產生衝撞及搓洗效應，使油泥中的油份往上懸浮，而於高溫較佳者例如135℃溫度下已達揮發狀態的廢水則變成蒸汽往上揮發，經三相分離機上方之冷凝段之後，還原成液態水體，再由物料輸送泵207輸送至該廢水處理步驟60進行廢水處理；而於此高溫較佳者例如135℃工作溫度下已變成石油氣之C1H4~C3H8等碳氫化合物則變成氣體往上懸浮，再藉由外部真空泵209對管線內部抽真空之效應，使石油氣經由管路被抽送經過冷凝器212冷凝，之後，再藉由真空罐208下方被抽離，導入下一階段石油氣氧化焚燬步驟30氧化及焚燬。 Please refer to Fig. 1 and Fig. 3, in the cyclone three-
而經過三相分離步驟處理之殘餘固體廢棄物則在該旋流三相分離機203艙底持續堆積，直至固體廢棄物堆積至一定之總量時，該旋流三相分離機203底部之閘刀閥開啟，殘留之固體廢棄物則落入下方之廢油渣暫存槽211，等待送入液態觸媒萃取步驟40進行後續之處理；而經由旋流三相分離機203處理後所回收之油料則直接送入回收油暫存槽210，待回收油暫存槽210達到高液位狀態，再將油料送入原油儲槽。 The residual solid waste treated by the three-phase separation step will continue to accumulate in the bilge of the cyclone three-
除了上述的主要設備之外，該旋流三相分離步驟20並配備有 一組熱交換器204，及連接附隨之物料輸送泵205及207，以及連接一組冷凝器212，用以該旋流三相分離步驟20物料輸送、熱交換或冷卻使用等，為使此一步驟符合設備可使用在Zone 1的規格要求，旋流三相分離機203及週邊所有的設備均依據NEMA或ATex IIB T4/T5的防爆規格要求而製作。 In addition to the above-mentioned main equipment, the cyclone three-
請參閱第1圖、第4圖，該石油氣氧化焚燬步驟30係以密閉式氧化及焚燬裝置為核心，其接續該旋流三相分離步驟20，將由該旋流三相分離步驟20所分離出來的廢石油氣藉由熱氧化焚毀裝置302內建的抽氣裝置將石油氣導入一石油氣回收槽301後，再藉由抽氣裝置抽送進入熱氧化焚毀裝置302之密閉式氧化槽中，經過氧化焚燬的廢氣則經過裝置的減排裝置後再排入大氣中。 Please refer to FIG. 1 and FIG. 4 , the LPG oxidation and
於作業中，如果石油氣氧化時的溫度未達到氧化焚燬所設定的溫度時，熱氧化焚燬裝置302所內建的進氣閥門會自行開啟，將外部已配置的丙烷氣導入與廢石油氣混合一起氧化焚燬，以便所排出的氣體再無任何廢石油氣殘存。 During the operation, if the temperature of the LPG oxidation does not reach the temperature set by the oxidation incineration, the air inlet valve built in the thermal
請參閱第1圖、第5圖，該液態觸媒萃取步驟40係以微氣泡萃取步驟41配合由外部攙入的液態觸媒，將由該旋流三相分離步驟20所排出的殘餘固體物中所夾帶的碳氫化合物包含瀝青質、石蠟、以及其它的碳氫化合物完全溶解及萃取出來，以便殘留的固體廢棄物不含碳氫化合物可直接掩埋或進行固化處理，而不會產生二次污染問題。 Please refer to Fig. 1 and Fig. 5, the liquid
此一部份之處理過程是接續該旋流三相分離步驟20的後續步驟，係將該旋流三相分離機203之主體裝置所排出的殘餘固體物輸送至廢油渣暫存槽402，再以輸送帶將殘餘固體廢棄物送入微氣泡萃取機401之處理槽中，此時槽中已先投入液態觸媒至工作液位，此一階段作業開始時，微氣泡發生機開始啟動，於槽中經由噴嘴將粒徑小於20micron(Ø0.02mm)之微細氣泡噴入槽中與殘餘固體物進行沖撞及清洗，攜帶液態觸媒之微氣泡則可深入固體廢棄物的微細的孔洞之中，將殘留在洞孔中的碳氫化合物包含瀝青質以及石蠟一起溶解及清洗出來，而與液態觸媒形成混合物；之後，步驟再持續投入殘餘固體廢棄物時，物料輸送泵406再將原已儲存在液態觸媒儲槽403的液態觸媒依據所投入的殘餘固體物的重量約千分之五(0.5%)的比例，將液態觸媒輸送入微氣泡萃取機401的清洗槽；而由於持續的投入物料即殘餘固體廢棄物以及液態觸媒，因此，在最高液位以上的液態觸媒以及碳氫化合物的混合物則會持續升高而產生溢流現象再進入溢流液暫存槽，待液位持續升高達到高液位時，再由物料輸送泵407將混合液輸送至回收油/液態觸媒混合物暫存槽405，等到液位升高至高液位時，再以物料輸送泵408輸送進入該液態觸媒回收步驟50。而經微氣泡萃取後的殘餘固體廢棄物則在萃取槽中慢慢堆積在萃取槽下方，等該批次的作業時間屆滿10分鐘時，則此一氣泡萃取步驟的控制器發出訊息停止進料，之後，電磁閥414開啟，槽體中的物料經由輸送泵412送入高速離心分離機411進行固液分離，被分離後的殘餘固體物則被推入固體物儲存槽404，而液體包含油及液太觸媒的混合物則導入混合液暫存槽410，隨後再由輸送泵413輸送至混合液混合槽405等待進一步處理。此一後續的固液分離步驟約為5分鐘，之後，電磁閥414關閉，物料即殘餘固體物又開始從402暫存槽開始進料，而液態觸媒也開始從液態觸媒儲槽開始輸送進入微氣泡萃取機，直至到達預設液位時，氣泡萃取機再度開始啟動運轉，進行下一批次的微氣泡萃取步驟。
This part of the treatment process is a subsequent step following the cyclone three-
由以上之說明可知，該微氣泡萃取步驟41即該液態觸媒萃取步驟40的核心技術，是以微氣泡沖激清洗工法配合液態觸媒以萃取殘存於殘留固體廢棄物表面或微細孔洞中的碳氫化合物，使得由該旋流三相分離步驟20所排出之殘餘固體物不再殘留任何碳氫化合物，包含瀝青質及石蠟，以達成將殘餘固體廢棄物中的碳氫化合物完全回收，不會再有造成任何二次污染的可能性，以達成將原油槽底泥做終極處理的目標。
It can be seen from the above description that the micro-bubble extraction step 41, that is, the core technology of the liquid
上述經過該微氣泡萃取步驟41處理後殘留之固體廢棄物已經不含任何碳氫化合物，尤其是其細微之孔洞之中已完全不殘存瀝青質、石蠟等物質，可以直接投入固體廢棄物儲桶404暫存，進而可直接掩埋或進行固化處理。
The above-mentioned solid waste remaining after the microbubble extraction step 41 does not contain any hydrocarbons, especially the fine pores are completely free of asphaltene, paraffin and other substances, and can be directly put into the solid
請參閱第1圖、第6圖，該液態觸媒回收步驟50是一個接續於該液態觸媒萃取步驟40之後，用於回收液態觸媒的步驟。此一步驟及裝置包含兩個以分子蒸餾器501、502為核心之分子蒸餾步驟。
Please refer to FIG. 1 and FIG. 6 , the liquid
作業時，來自該液態觸媒萃取步驟40之物料輸送泵408將液態觸媒及回收油混合物送經預熱器H1，經過緩慢的溫度傳遞後加溫至60℃後再進入第一個分子蒸餾器501，旋即被分子蒸餾器持續旋轉的刮板刮至汽缸壁形成一大約0.5mm~1mm厚度的薄膜，而由於外部的真空泵VGA-1或VGA-2持續透過冷井的管道對分子蒸餾器501內部持續抽真空，因此分子蒸餾器501的內部工作壓力可保持在100Pa以下，於此工作壓力下，形成薄膜黏附於分子蒸餾器501汽缸壁的混合液於分子自由行程(Molecular Free Path)效應下，部份已經達到沸點(Boling point)的分子亦即液態觸媒已經開始變成揮發氣體(Mist)，由於分子蒸餾器501持續經由外部抽真空，因此，通往外部管道的壓力形成一個急速下降的壓差，而這些已經蒸發的液態觸媒分子(Molecular)即霧狀液態觸媒則往壓力較低的管道出口移動，但移動至分子蒸餾器501本體中央部位時，就被一組內置冷凝器阻擋，由於內置冷凝器的冷凝管表面溫度為略低於常溫之水溫，因此這些已經被蒸發的液態觸媒分子與冷凝管道接觸後則立即被冷凝回復成液態，再循分子蒸餾器501下方的出口落入暫存槽，待高液位時再輸送回步驟40之液態觸媒儲槽403(請參閱圖5)，而極少部份未能於內置冷凝器被補捉的液態觸媒分子則會循著抽真空的管線通道進入連接於分子蒸餾器501外部的冷井，而被冷凝下來，再落入下方的回收緩衝槽Z1中，等液位達到高液位時，再輸送至外部的液態觸媒暫存槽V5。 During operation, the
沸點較高的回收油及原油、凝析油或柴油、油基潤滑劑，則於工作溫度為60℃及100Pa工作壓力下仍無法被蒸發，因此，會循著分子蒸餾器501下方側邊的出口流入下方的半成品緩衝槽V1，等待送至第二階段的分子蒸餾步驟；而極少量的液態觸媒於第一分子蒸餾步驟中，或由於進料速度之變化、冷凝速度不足、或分子蒸餾器本體蒸發率的問題沒有被完全回收，則與油料一起落入下方之緩衝槽V1與回收油及油基潤滑劑等物料形成混合液，而被送入第二段的分子蒸餾步驟加以回收，以避免產生資源浪費的問題。 The recovered oil, crude oil, condensate or diesel oil, and oil-based lubricants with higher boiling points cannot be evaporated under the working temperature of 60°C and the working pressure of 100Pa. The outlet flows into the semi-finished product buffer tank V1 below, waiting to be sent to the molecular distillation step of the second stage; while a very small amount of liquid catalyst is in the first molecular distillation step, or due to changes in the feed rate, insufficient condensation rate, or molecular distillation If the evaporation rate of the main body of the device is not completely recovered, it will fall into the buffer tank V1 below together with the oil to form a mixed solution with recovered oil and oil-based lubricants, and then be sent to the second stage of the molecular distillation step for recovery. To avoid the problem of waste of resources.
而在第二階段的分子蒸餾步驟是一備用的步驟，目的是防止液態觸媒因為進料量需大幅增加，或是油泥中的固體物含量突然大幅度增加，以致於所添加的液態觸媒也大幅增加，此時，作業參數就需要更動，否則大量增加的觸媒就無法完全被回收，會造成操作費用的大幅提高；第 二分子蒸餾步驟的配置及作業原理則與第一個分子蒸餾步驟完全相同。 The molecular distillation step in the second stage is a backup step, the purpose is to prevent the liquid catalyst from being greatly increased due to the large increase in the feed amount or the sudden and large increase in the solid content in the sludge, so that the added liquid catalyst It is also greatly increased. At this time, the operating parameters need to be changed. Otherwise, the large-scale increase of the catalyst cannot be completely recovered, which will cause a substantial increase in operating costs. The configuration and operating principle of the second molecular distillation step are the same as the first molecular distillation. The steps are exactly the same.
請參閱第6圖，第二階段的分子蒸餾步驟單元包含有一預熱器H4、一分子蒸餾器502、一冷井H6、一個與分子蒸餾器501共用的真空泵VGA-1及VGA-2(備用)、四物料暫存槽V3~V4及V6~V7、四物料輸送泵P4~P7、以及一回收油儲槽503。 Please refer to FIG. 6, the molecular distillation step unit of the second stage includes a preheater H4, a molecular still 502, a cold well H6, and a vacuum pump VGA-1 and VGA-2 (standby) shared with the
除了上述兩個分子蒸餾單元之外，此一步驟50尚包含一個公用的冰水系統504，以提供低溫冷凝水給冷井以回收外逸的液態觸媒分子；一個冷卻系統505，以便將冷卻水降溫以適合現場使用；一個中央加熱流體系統506，以便產生蒸汽，以間接對進入該液態觸媒回收步驟50的液態觸媒及回收油的混合物進行加熱，以符作業需求。 In addition to the above two molecular distillation units, this
請參閱第1圖、第7圖，該廢水處理步驟60係接續於該旋流三相分離步驟20之後，做為一個輔助的步驟，以便將產自該旋流三相分離步驟20的廢水做完整處理，以免廢水外流產生二次污染問題。 Please refer to FIG. 1 and FIG. 7, the
該廢水處理步驟60包含三個物理性的廢水處理單元，即一精密油水分離機605、一微過濾器608、及一陰陽離子交換器611，及其它設備包含一廢水暫存槽601、一回收油暫存槽603、數個廢水進料輸送泵602、604、607、610及二緩衝槽606、609。 The
作業時，由該旋流三相分離步驟20所產出之廢水被輸送至廢水暫存槽601，待達到高液位之後被輸送泵604自動抽進入精密油水分離機605進行處理，經過處理後之廢水則被送入緩衝槽606暫存，等到儲槽達到高液位後，再由廢水進料輸送泵607將廢水送入微過濾器608，以去除粒徑小於0.8Micron的微小油滴，之後廢水被導入緩衝槽609暫存，等儲槽液位 升高至高液位時，再以廢水進料輸送泵610將廢水送入陰陽離子交換器611做最終之處理，以確保經處理後之廢水不含任何油份或者異味。 During operation, the waste water produced by the cyclone three-
由於該旋流三相分離步驟20需使用蒸汽，而蒸汽則需以水為介質經加熱超過100℃才能產生蒸汽，於該旋流三相分離步驟20所使用之蒸汽則是溫度為135℃過熱蒸汽，但也需以水為物料加熱所得，因此，於該廢水處理步驟60所回收之廢水最佳的處理方式是送入該旋流三相分離步驟20所配備的軟水器中做預處理，之後再送入鍋爐中加熱使成為過熱蒸汽，如此循環使用既能避免任何可能的二次污染，且可將回收水提供給該旋流三相分離步驟20做為水源，可達成資源回收再利用的目標。 Since the cyclone three-
以上為本案所舉之實施例，僅為便於說明而設，當不能以此限制本案之意義，即大凡依所列申請專利範圍所為之各種變換設計，均應包含在本案之專利範圍中。 The above are examples of this case, which are only for the convenience of illustration, and should not limit the meaning of this case, that is, all kinds of transformation designs based on the listed scope of the patent application should be included in the scope of the patent of this case.
10‧‧‧油泥均質化預處理步驟 10‧‧‧Sludge homogenization pretreatment steps
101‧‧‧凝析油/柴油儲槽 101‧‧‧Condensate/diesel storage tank
103‧‧‧油泥過濾篩 103‧‧‧Sludge filter
105‧‧‧油泥預熱槽 105‧‧‧Sludge preheating tank
20‧‧‧旋流三相分離步驟 20‧‧‧Swirl three-phase separation steps
201‧‧‧油泥攪拌槽 201‧‧‧Sludge mixing tank
203‧‧‧旋流三相分離機 203‧‧‧Swirl three-phase separator
210‧‧‧回收油暫存槽 210‧‧‧Temporary storage tank for recovered oil
30‧‧‧石油氣氧化焚燬步驟 30‧‧‧LPG Oxidative Incineration Steps
301‧‧‧石油氣回收槽 301‧‧‧LPG recovery tank
302‧‧‧石油氣氧化焚燬裝置 302‧‧‧Petroleum gas oxidation incineration device
40‧‧‧液態觸媒萃取步驟 40‧‧‧Liquid catalyst extraction step
403‧‧‧液態觸媒儲槽 403‧‧‧Liquid catalyst storage tank
41‧‧‧微氣泡萃取步驟 41‧‧‧Microbubble extraction steps
405‧‧‧回收油/液態觸媒混合物暫存槽 405‧‧‧Temporary storage tank for recovered oil/liquid catalyst mixture
50‧‧‧液態觸媒回收步驟 50‧‧‧Liquid catalyst recovery steps
501‧‧‧第一段分子蒸餾步驟 501‧‧‧First Molecular Distillation Step
502‧‧‧第二段分子蒸餾步驟 502‧‧‧Second stage molecular distillation step
503‧‧‧回收油儲槽 503‧‧‧Recovery Oil Storage Tank
60‧‧‧廢水處理步驟 60‧‧‧Wastewater treatment steps
601‧‧‧廢水暫存槽 601‧‧‧Wastewater temporary storage tank
605‧‧‧精密油水分離機 605‧‧‧Precision oil-water separator
608‧‧‧微過濾器 608‧‧‧Micro Filter
611‧‧‧陰陽離子交換槽 611‧‧‧Anion and cation exchange tank
Claims (10)
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| CN101684028A (en) * | 2008-09-28 | 2010-03-31 | 张伟民 | Method and device for disposing cutting waste of silicon crystal board |
| TW201700412A (en) * | 2015-06-22 | 2017-01-01 | 國立宜蘭大學 | A CO-treatment process of sludge |
| CN108275859A (en) * | 2018-01-23 | 2018-07-13 | 郑州云启工业设备技术有限公司 | A kind of continuous greasy filth environment-friendly treating process |
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| CN101684028A (en) * | 2008-09-28 | 2010-03-31 | 张伟民 | Method and device for disposing cutting waste of silicon crystal board |
| TW201700412A (en) * | 2015-06-22 | 2017-01-01 | 國立宜蘭大學 | A CO-treatment process of sludge |
| CN108275859A (en) * | 2018-01-23 | 2018-07-13 | 郑州云启工业设备技术有限公司 | A kind of continuous greasy filth environment-friendly treating process |
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