CN221815339U - A device for producing high-purity anhydrous ethanol - Google Patents
A device for producing high-purity anhydrous ethanol Download PDFInfo
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 380
- 239000012466 permeate Substances 0.000 claims abstract description 78
- 239000012528 membrane Substances 0.000 claims abstract description 51
- 239000000047 product Substances 0.000 claims abstract description 46
- 238000000926 separation method Methods 0.000 claims abstract description 41
- 239000002994 raw material Substances 0.000 claims abstract description 38
- 239000007788 liquid Substances 0.000 claims abstract description 20
- 238000007670 refining Methods 0.000 claims abstract description 17
- 235000019441 ethanol Nutrition 0.000 claims abstract 30
- 238000001816 cooling Methods 0.000 claims description 15
- 230000000712 assembly Effects 0.000 claims 1
- 238000000429 assembly Methods 0.000 claims 1
- 238000007599 discharging Methods 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 claims 1
- 238000000746 purification Methods 0.000 abstract description 6
- 239000002699 waste material Substances 0.000 abstract description 6
- 238000011084 recovery Methods 0.000 abstract description 4
- 238000001704 evaporation Methods 0.000 abstract description 2
- 230000008020 evaporation Effects 0.000 abstract description 2
- 238000004821 distillation Methods 0.000 description 35
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 21
- 230000018044 dehydration Effects 0.000 description 7
- 238000006297 dehydration reaction Methods 0.000 description 7
- LYCAIKOWRPUZTN-UHFFFAOYSA-N ethylene glycol Substances OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 238000009833 condensation Methods 0.000 description 5
- 230000005494 condensation Effects 0.000 description 5
- 238000000034 method Methods 0.000 description 4
- 239000010865 sewage Substances 0.000 description 4
- 239000006227 byproduct Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000011144 upstream manufacturing Methods 0.000 description 3
- 101001121408 Homo sapiens L-amino-acid oxidase Proteins 0.000 description 2
- 102100026388 L-amino-acid oxidase Human genes 0.000 description 2
- 101100233916 Saccharomyces cerevisiae (strain ATCC 204508 / S288c) KAR5 gene Proteins 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 101100012902 Saccharomyces cerevisiae (strain ATCC 204508 / S288c) FIG2 gene Proteins 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 238000010533 azeotropic distillation Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- IDGUHHHQCWSQLU-UHFFFAOYSA-N ethanol;hydrate Chemical compound O.CCO IDGUHHHQCWSQLU-UHFFFAOYSA-N 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 238000000895 extractive distillation Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000005373 pervaporation Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
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Abstract
Description
技术领域Technical Field
本实用新型属于乙醇纯化技术领域，具体涉及一种生产高纯度无水乙醇的装置。The utility model belongs to the technical field of ethanol purification, and in particular relates to a device for producing high-purity anhydrous ethanol.
背景技术Background Art
在煤制乙二醇工艺中，除了主产品乙二醇外，会有加氢产生的副产物如乙醇作为副产品被乙二醇精馏系统分离出来。受精馏塔分离效果和技术操作的限制，乙醇在分离过程中大多只能作为浓度为95％左右的粗品乙醇产品外售，其价值远小于高纯乙醇。In the coal-to-ethylene glycol process, in addition to the main product ethylene glycol, byproducts such as ethanol produced by hydrogenation are separated as byproducts by the ethylene glycol distillation system. Limited by the separation effect of the distillation tower and technical operation, ethanol can only be sold as a crude ethanol product with a concentration of about 95% during the separation process, and its value is far less than that of high-purity ethanol.
目前，工业上无水乙醇的生产方法主要有恒沸精馏、萃取精馏、吸附和膜分离等方法。其中，膜分离法主要是指渗透汽化脱水，其可以分离乙醇水溶液，得到乙醇蒸汽和渗透液蒸汽，乙醇蒸汽冷凝后得到无水乙醇。然而，乙醇蒸汽通常由循环冷却水进行冷却，循环冷却水吸热后水温升高有限，很难被重新利用，因此，乙醇蒸汽这部分热量未被回收利用起来，存在能源浪费的现象。At present, the main methods for producing anhydrous ethanol in industry include azeotropic distillation, extractive distillation, adsorption and membrane separation. Among them, membrane separation mainly refers to pervaporation dehydration, which can separate ethanol-water solution to obtain ethanol vapor and permeate vapor, and ethanol vapor is condensed to obtain anhydrous ethanol. However, ethanol vapor is usually cooled by circulating cooling water, and the water temperature rises only slightly after the circulating cooling water absorbs heat, and it is difficult to reuse. Therefore, the heat of ethanol vapor is not recycled, resulting in energy waste.
实用新型内容Utility Model Content
本实用新型意在提供一种生产高纯度无水乙醇的装置，以解决采用膜分离法纯化乙醇时存在能源浪费的问题。The utility model aims to provide a device for producing high-purity anhydrous ethanol to solve the problem of energy waste when purifying ethanol by membrane separation method.
为了达到上述目的，本实用新型的方案为：一种生产高纯度无水乙醇的装置，包括乙醇精制塔、原料储罐和膜分离机组，还包括预热器、蒸发器、渗透液处理机组、精馏塔、塔顶冷凝器、冷凝液储罐、乙醇脱轻塔和乙醇成品储罐，所述乙醇精制塔塔顶出口与原料储罐连接，原料储罐内的乙醇溶液经预热器和蒸发器进入膜分离机组，膜分离机组的渗透液出口与所述渗透液处理机组的进口连接，膜分离组件的醇出口与预热器的进口连接，预热器的出口与所述精馏塔连接，精馏塔的塔顶出口与所述塔顶冷凝器的进口连接，塔顶冷凝器的出口与所述冷凝液储罐连接，冷凝液储罐的出口分别与精馏塔的塔顶和所述乙醇脱轻塔的进口连接，精馏塔的塔釜出口分别与所述原料储罐、乙醇成品储罐和乙醇精制塔连接。In order to achieve the above-mentioned purpose, the scheme of the utility model is: a device for producing high-purity anhydrous ethanol, comprising an ethanol refining tower, a raw material storage tank and a membrane separation unit, and also comprising a preheater, an evaporator, a permeate treatment unit, a distillation tower, a tower top condenser, a condensate storage tank, an ethanol light removal tower and an ethanol finished product storage tank, the tower top outlet of the ethanol refining tower is connected to the raw material storage tank, the ethanol solution in the raw material storage tank enters the membrane separation unit through the preheater and the evaporator, the permeate outlet of the membrane separation unit is connected to the inlet of the permeate treatment unit, the alcohol outlet of the membrane separation assembly is connected to the inlet of the preheater, the outlet of the preheater is connected to the distillation tower, the tower top outlet of the distillation tower is connected to the inlet of the tower top condenser, the outlet of the tower top condenser is connected to the condensate storage tank, the outlet of the condensate storage tank is respectively connected to the tower top of the distillation tower and the inlet of the ethanol light removal tower, and the tower bottom outlet of the distillation tower is respectively connected to the raw material storage tank, the ethanol finished product storage tank and the ethanol refining tower.
本方案的工作原理及有益效果在于：本方案中，乙醇精制塔生产的低纯度乙醇溶液(低纯度乙醇溶液是指95％乙醇溶液)进入原料储罐，后在预热器内与经膜分离组件得到的混合醇蒸汽进行热交换，低浓度乙醇溶液的温度升高，其在蒸发器内蒸发为蒸汽所需的热量减少，从而实现混合醇蒸汽的热量回收利用，避免该部分能源浪费；而混合醇蒸汽的温度降低后进入精馏塔内，精馏塔的塔顶采出含甲醇的乙醇蒸汽，经塔顶冷凝器冷凝后进入冷凝液储罐，冷凝液部分回到精馏塔，另一部分送至乙醇脱轻塔，从而分离回收甲醇。另外，由于精馏塔的塔釜出口分别与原料储罐、乙醇成品储罐和乙醇精制塔连接，因此，当乙醇纯度达标时，乙醇作为成品进入乙醇成品罐内储存，当乙醇纯度未达标时，乙醇进入原料储罐继续进行膜分离脱水或者进入乙醇精制塔精馏，从而使得纯度未达标的乙醇有去路，避免精馏塔内液体过多。The working principle and beneficial effects of this scheme are as follows: in this scheme, the low-purity ethanol solution (the low-purity ethanol solution refers to the 95% ethanol solution) produced by the ethanol refining tower enters the raw material storage tank, and then undergoes heat exchange with the mixed alcohol vapor obtained through the membrane separation component in the preheater. The temperature of the low-concentration ethanol solution increases, and the heat required for its evaporation into steam in the evaporator is reduced, thereby realizing heat recovery and utilization of the mixed alcohol vapor, and avoiding the waste of this part of energy; and after the temperature of the mixed alcohol vapor is reduced, it enters the distillation tower, and the ethanol vapor containing methanol is extracted from the top of the distillation tower, and enters the condensate storage tank after condensation by the top condenser. Part of the condensate returns to the distillation tower, and the other part is sent to the ethanol light removal tower, so as to separate and recover the methanol. In addition, since the bottom outlet of the distillation tower is respectively connected to the raw material storage tank, the ethanol finished product storage tank and the ethanol refining tower, when the ethanol purity meets the standard, the ethanol enters the ethanol finished product tank for storage as a finished product. When the ethanol purity does not meet the standard, the ethanol enters the raw material storage tank to continue membrane separation and dehydration or enters the ethanol refining tower for distillation, so that the ethanol that does not meet the purity standard has a way out, avoiding excessive liquid in the distillation tower.
综上所述，本方案通过膜分离机组实现乙醇的脱水，并通过精馏塔实现乙醇的进一步纯化，能够得到纯度近乎100％的无水乙醇产品，增加了副产品的价值。并且，膜分离机组产生的混合醇蒸汽能够对进入膜分离机组前的低浓度乙醇溶液进行预热，避免了混合醇蒸汽的热量被浪费。此外，本方案还实现了甲醇的回收。In summary, this solution achieves dehydration of ethanol through a membrane separation unit and further purification of ethanol through a distillation tower, and can obtain anhydrous ethanol products with a purity of nearly 100%, thereby increasing the value of by-products. In addition, the mixed alcohol vapor generated by the membrane separation unit can preheat the low-concentration ethanol solution before entering the membrane separation unit, thereby avoiding the waste of heat of the mixed alcohol vapor. In addition, this solution also achieves the recovery of methanol.
可选地，所述渗透液处理机组包括渗透液冷凝器、渗透液罐、真空机组、渗透液泵、尾气冷凝器和尾冷罐，渗透液冷凝器的进口与膜分离机组的渗透液出口连接，渗透液冷凝器的出口与渗透液罐连接，真空机组的进口与渗透液罐的顶端连接，渗透液泵用于排出渗透液罐内的渗透液，尾气冷凝器与真空机组的出口连接，尾气冷凝器的出口与尾冷罐连接，尾冷罐的顶端连接有不凝尾气管。Optionally, the permeate treatment unit includes a permeate condenser, a permeate tank, a vacuum unit, a permeate pump, a tail gas condenser and a tail cooling tank, the inlet of the permeate condenser is connected to the permeate outlet of the membrane separation unit, the outlet of the permeate condenser is connected to the permeate tank, the inlet of the vacuum unit is connected to the top of the permeate tank, the permeate pump is used to discharge the permeate in the permeate tank, the tail gas condenser is connected to the outlet of the vacuum unit, the outlet of the tail gas condenser is connected to the tail cooling tank, and the top of the tail cooling tank is connected with a non-condensable tail gas pipe.
本方案中，真空机组抽真空以形成膜上下游两侧组份的蒸汽分压差，以此作为推动力实现原料中水分和少量醇的有效渗透，渗透液蒸汽在真空机组的抽吸下经渗透液冷凝器冷凝成渗透液，渗透液进入渗透液罐，经渗透液泵送至污水处理站。而渗透液冷凝器中的不凝气在真空机组的抽吸下进入尾气冷凝器进行冷凝，得到的冷凝液进入尾冷罐，不凝气则经不凝尾气管排放至尾气总管。In this scheme, the vacuum unit draws a vacuum to form a vapor partial pressure difference between the components on both sides of the membrane, which is used as a driving force to achieve effective permeation of water and a small amount of alcohol in the raw material. The permeate vapor is condensed into permeate through the permeate condenser under the suction of the vacuum unit. The permeate enters the permeate tank and is pumped to the sewage treatment station. The non-condensable gas in the permeate condenser enters the tail gas condenser under the suction of the vacuum unit for condensation. The condensate obtained enters the tail cooling tank, and the non-condensable gas is discharged to the tail gas main pipe through the non-condensable tail gas pipe.
可选地，所述膜分离机组的数量为两组，每组膜分离机组均包括两个以上的膜组件。Optionally, there are two membrane separation units, and each membrane separation unit includes more than two membrane modules.
本方案中，膜分离机组的数量为两组，单位时间内对乙醇的处理量增多，确保乙醇脱水效率。另外，每组膜分离机组包括两个以上的膜组件，确保对乙醇的脱水效果。In this scheme, the number of membrane separation units is two, and the processing amount of ethanol per unit time is increased to ensure the ethanol dehydration efficiency. In addition, each membrane separation unit includes more than two membrane modules to ensure the dehydration effect of ethanol.
可选地，所述渗透液处理机组的数量为两组，两组渗透液处理机组中的渗透液罐连通。Optionally, there are two permeate processing units, and the permeate tanks in the two permeate processing units are connected.
本方案中，两组渗透液处理机组中的渗透液罐连通时，真空机组的数量为一组即可，渗透液泵的数量也为一台即可，减少设备的投入成本。In this solution, when the permeate tanks in two groups of permeate treatment units are connected, the number of vacuum units can be one group, and the number of permeate pumps can be one, thereby reducing the investment cost of the equipment.
可选地，所述精馏塔与乙醇成品储罐之间设有中间罐，中间罐的数量为两个以上，两个以上的中间罐并联设置，中间罐与乙醇成品储罐连接，且中间罐与乙醇成品储罐之间设有阀门Ⅰ和乙醇成品泵。Optionally, an intermediate tank is provided between the distillation tower and the ethanol finished product storage tank, the number of the intermediate tanks is more than two, more than two intermediate tanks are arranged in parallel, the intermediate tank is connected to the ethanol finished product storage tank, and a valve I and an ethanol finished product pump are provided between the intermediate tank and the ethanol finished product storage tank.
本方案中，当乙醇纯度未达标，但乙醇出路未及时切换时，将会导致纯度未达标的乙醇进入乙醇成品储罐的路线内，此时，中间罐的设计则能够暂时存放这些纯度未达标的乙醇，避免未达标的乙醇直接进入乙醇成品储罐而影响乙醇成品储罐内的乙醇品质。而并联设置的中间罐，能够在上一中间罐装满后使用下一中间罐。In this solution, when the purity of ethanol does not meet the standard, but the ethanol outlet is not switched in time, the ethanol with substandard purity will enter the route of the ethanol finished product storage tank. At this time, the design of the intermediate tank can temporarily store the ethanol with substandard purity, so as to prevent the ethanol with substandard purity from directly entering the ethanol finished product storage tank and affecting the quality of the ethanol in the ethanol finished product storage tank. The intermediate tanks set in parallel can use the next intermediate tank after the previous intermediate tank is full.
可选地，所述中间罐与原料储罐连接，且中间罐与原料储罐之间设有阀门Ⅱ和乙醇回料泵。Optionally, the intermediate tank is connected to the raw material storage tank, and a valve II and an ethanol return pump are provided between the intermediate tank and the raw material storage tank.
本方案中，中间罐内的乙醇装满时，检测中间罐内乙醇的纯度，若纯度达标，则将中间罐内的乙醇泵入乙醇成品储罐内；若纯度不达标，则将中间罐内的乙醇泵入原料储罐，重新进入脱水纯化过程。In this scheme, when the ethanol in the intermediate tank is full, the purity of the ethanol in the intermediate tank is tested. If the purity meets the standard, the ethanol in the intermediate tank is pumped into the ethanol finished product storage tank; if the purity does not meet the standard, the ethanol in the intermediate tank is pumped into the raw material storage tank and re-enters the dehydration purification process.
可选地，所述精馏塔与乙醇成品储罐之间设有乙醇冷凝器。Optionally, an ethanol condenser is provided between the distillation tower and the ethanol product storage tank.
本方案中，利用乙醇冷凝器冷却经精馏塔塔釜出口采出的乙醇，降低乙醇的温度。In this scheme, an ethanol condenser is used to cool the ethanol extracted from the outlet of the distillation tower kettle to reduce the temperature of the ethanol.
可选地，所述塔顶冷凝器包括一级冷凝器和二级冷凝器，一级冷凝器的进口与精馏塔的塔顶出口连接，一级冷凝器的出口与冷凝液储罐连接，二级冷凝器的进口与一级冷凝器的不凝气出口连接，二级冷凝器的出口与冷凝液储罐连接，且冷凝液储罐的顶端与二级冷凝器的进口连接。Optionally, the top condenser includes a primary condenser and a secondary condenser, the inlet of the primary condenser is connected to the top outlet of the distillation tower, the outlet of the primary condenser is connected to a condensate storage tank, the inlet of the secondary condenser is connected to the non-condensable gas outlet of the primary condenser, the outlet of the secondary condenser is connected to the condensate storage tank, and the top of the condensate storage tank is connected to the inlet of the secondary condenser.
本方案中，含甲醇的乙醇蒸汽进入一级冷凝器后，部分冷凝成液体进入冷凝液储罐，另一部分未凝的蒸汽，部分进入二级冷凝器(二级冷凝器采用冷冻水作为冷却介质)内继续冷凝，另一部分进入冷凝液储罐内。由于冷凝液储罐的顶端与二级冷凝器的进口连接，因此，冷凝液储罐内的蒸汽也可以进入二级冷凝器内进行冷凝。In this scheme, after the ethanol vapor containing methanol enters the primary condenser, part of it is condensed into liquid and enters the condensate storage tank, and the other part of the uncondensed vapor enters the secondary condenser (the secondary condenser uses chilled water as a cooling medium) to continue condensing, and the other part enters the condensate storage tank. Since the top of the condensate storage tank is connected to the inlet of the secondary condenser, the vapor in the condensate storage tank can also enter the secondary condenser for condensation.
附图说明BRIEF DESCRIPTION OF THE DRAWINGS
图1为本实用新型实施例一中一种生产高纯度无水乙醇的装置的结构示意图；FIG1 is a schematic diagram of the structure of a device for producing high-purity anhydrous ethanol in Example 1 of the utility model;
图2为图1中A的放大示意图；FIG2 is an enlarged schematic diagram of A in FIG1 ;
图3为本实用新型实施例二中一种生产高纯度无水乙醇的装置的结构示意图。FIG3 is a schematic diagram of the structure of a device for producing high-purity anhydrous ethanol in Example 2 of the present utility model.
具体实施方式DETAILED DESCRIPTION
下面通过具体实施方式进一步详细说明：The following is further described in detail through specific implementation methods:
说明书附图中的标记包括：乙醇精制塔1、原料储罐2、膜分离机组3、预热器4、蒸发器5、渗透液冷凝器6、渗透液罐7、真空机组8、渗透液泵9、尾气冷凝器10、尾冷罐11、精馏塔12、一级冷凝器13、二级冷凝器14、冷凝液储罐15、乙醇脱轻塔16、乙醇成品储罐17、乙醇冷凝器18、中间罐19、乙醇成品泵20、乙醇回料泵21。The symbols in the drawings of the specification include: ethanol refining tower 1, raw material storage tank 2, membrane separation unit 3, preheater 4, evaporator 5, permeate condenser 6, permeate tank 7, vacuum unit 8, permeate pump 9, tail gas condenser 10, tail cooling tank 11, distillation tower 12, primary condenser 13, secondary condenser 14, condensate storage tank 15, ethanol light removal tower 16, ethanol finished product storage tank 17, ethanol condenser 18, intermediate tank 19, ethanol finished product pump 20, ethanol return pump 21.
实施例一Embodiment 1
本实施例基本如图1和图2所示：一种生产高纯度无水乙醇的装置，包括乙醇精制塔1、原料储罐2、膜分离机组3、预热器4、蒸发器5、渗透液处理机组、精馏塔12、塔顶冷凝器、冷凝液储罐15、乙醇脱轻塔16和乙醇成品储罐17。This embodiment is basically as shown in Figures 1 and 2: a device for producing high-purity anhydrous ethanol, including an ethanol refining tower 1, a raw material storage tank 2, a membrane separation unit 3, a preheater 4, an evaporator 5, a permeate treatment unit, a distillation tower 12, a top condenser, a condensate storage tank 15, an ethanol light removal tower 16 and an ethanol finished product storage tank 17.
乙醇精制塔1的塔顶出口与原料储罐2连接，原料储罐2与预热器4的管程进口连接，预热器4的管程出口与蒸发器5的进口连接，蒸发器5的出口与膜分离机组3的进口连接，如此，原料储罐2内的低浓度乙醇溶液即可经预热器4和蒸发器5进入膜分离机组3。膜分离机组3的数量为两组，每组膜分离机组3均包括两个以上的膜组件，两个以上的膜组件串联，本实施例中，每组膜分离机组3中的膜组件的数量为六个。The top outlet of the ethanol refining tower 1 is connected to the raw material storage tank 2, the raw material storage tank 2 is connected to the tube side inlet of the preheater 4, the tube side outlet of the preheater 4 is connected to the inlet of the evaporator 5, and the outlet of the evaporator 5 is connected to the inlet of the membrane separation unit 3, so that the low-concentration ethanol solution in the raw material storage tank 2 can enter the membrane separation unit 3 through the preheater 4 and the evaporator 5. The number of membrane separation units 3 is two, each group of membrane separation units 3 includes more than two membrane modules, and the more than two membrane modules are connected in series. In this embodiment, the number of membrane modules in each group of membrane separation units 3 is six.
膜分离机组3的渗透液出口与渗透液处理机组的进口连接，渗透液处理机组的数量为两组，每组渗透液处理机组均包括渗透液冷凝器6和渗透液罐7，其中一组渗透液处理机组还包括真空机组8、尾气冷凝器10和尾冷罐11，另一组渗透液处理机组还包括渗透液泵9，渗透液冷凝器6的进口与膜分离机组3的渗透液出口连接，渗透液冷凝器6的出口与渗透液罐7连接，两组渗透液处理机组中的渗透液罐7相互连通，真空机组8的进口与一渗透液罐7的顶端连接，渗透液泵9的进口与一渗透液罐7的底端连接，用于将渗透液罐7内的渗透液泵9送至污水处理站；真空机组8的出口与尾气冷凝器10的进口连接，尾气冷凝器10的出口与尾冷罐11连接，尾冷罐11的顶端连接有不凝尾气管，从而将不凝尾气送至尾气总管内。The permeate outlet of the membrane separation unit 3 is connected to the inlet of the permeate treatment unit. There are two groups of permeate treatment units. Each group of permeate treatment units includes a permeate condenser 6 and a permeate tank 7. One group of permeate treatment units also includes a vacuum unit 8, a tail gas condenser 10 and a tail cooling tank 11. The other group of permeate treatment units also includes a permeate pump 9. The inlet of the permeate condenser 6 is connected to the permeate outlet of the membrane separation unit 3, and the outlet of the permeate condenser 6 is connected to the permeate tank 7. The permeate tanks 7 in the two permeate treatment units are interconnected, the inlet of the vacuum unit 8 is connected to the top of a permeate tank 7, and the inlet of the permeate pump 9 is connected to the bottom of a permeate tank 7, so as to deliver the permeate pump 9 in the permeate tank 7 to the sewage treatment station; the outlet of the vacuum unit 8 is connected to the inlet of the tail gas condenser 10, and the outlet of the tail gas condenser 10 is connected to the tail cooling tank 11, and the top of the tail cooling tank 11 is connected with a non-condensable tail gas pipe, so as to deliver the non-condensable tail gas to the tail gas main pipe.
膜分离组件的醇出口与预热器4的壳程进口连接，预热器4的壳程出口与述精馏塔12连接，精馏塔12的塔顶出口与塔顶冷凝器的进口连接，塔顶冷凝器的出口与冷凝液储罐15连接；本实施例中，塔顶冷凝器包括一级冷凝器13和二级冷凝器14，一级冷凝器13的进口与精馏塔12的塔顶出口连接，一级冷凝器13的出口与冷凝液储罐15连接，二级冷凝器14的进口与一级冷凝器13的不凝气出口连接，二级冷凝器14的出口与冷凝液储罐15连接，且冷凝液储罐15的顶端与二级冷凝器14的进口连接，二级冷凝器14的不凝气出口以供二级冷凝器14内的不凝气排放至尾气总管内，维持精馏塔12塔压稳定。The alcohol outlet of the membrane separation component is connected to the shell side inlet of the preheater 4, the shell side outlet of the preheater 4 is connected to the distillation tower 12, the top outlet of the distillation tower 12 is connected to the inlet of the top condenser, and the outlet of the top condenser is connected to the condensate storage tank 15; in the present embodiment, the top condenser comprises a primary condenser 13 and a secondary condenser 14, the inlet of the primary condenser 13 is connected to the top outlet of the distillation tower 12, the outlet of the primary condenser 13 is connected to the condensate storage tank 15, the inlet of the secondary condenser 14 is connected to the non-condensable gas outlet of the primary condenser 13, the outlet of the secondary condenser 14 is connected to the condensate storage tank 15, and the top of the condensate storage tank 15 is connected to the inlet of the secondary condenser 14, the non-condensable gas outlet of the secondary condenser 14 is for the non-condensable gas in the secondary condenser 14 to be discharged into the tail gas main pipe, so as to maintain the tower pressure of the distillation tower 12 stable.
冷凝液储罐15的出口分别与精馏塔12的塔顶和乙醇脱轻塔16的进口连接，如此，冷凝液储罐15内的部分冷凝液回到精馏塔12，另一部分冷凝液被送至乙醇脱轻塔16。精馏塔12的塔釜出口分别与原料储罐2、乙醇成品储罐17和乙醇精制塔1连接，且精馏塔12与乙醇成品储罐17之间设有乙醇冷凝器18，用于冷却从精馏塔12塔釜出口采出的乙醇。The outlet of the condensate storage tank 15 is connected to the top of the distillation tower 12 and the inlet of the ethanol light removal tower 16, respectively. In this way, part of the condensate in the condensate storage tank 15 returns to the distillation tower 12, and the other part of the condensate is sent to the ethanol light removal tower 16. The tower bottom outlet of the distillation tower 12 is connected to the raw material storage tank 2, the ethanol product storage tank 17 and the ethanol refining tower 1, respectively, and an ethanol condenser 18 is provided between the distillation tower 12 and the ethanol product storage tank 17 for cooling the ethanol extracted from the tower bottom outlet of the distillation tower 12.
运行时，乙醇精制塔1的塔顶出口采出的乙醇蒸汽经冷凝后得到低浓度乙醇溶液(低浓度乙醇溶液的乙醇纯度约为95％)，部分低浓度乙醇溶液进入原料储罐2。原料储罐2内的低浓度乙醇溶液进入预热器4内，再进入蒸发器5，在蒸发器5内吸热转为原料蒸汽，随后原料蒸汽并联进入两组膜分离机组3中。在真空机组8的抽吸下，膜组件上游侧和膜组件下游侧的蒸汽分压差，原料蒸汽中的水分和少量乙醇等醇类物经膜组件由膜上游侧渗透至膜下游侧，最后一级膜组件上游侧得到含水量≤0.3wt％的混合醇蒸汽，膜下游侧的渗透液蒸汽进入渗透液冷凝器6，冷凝后的渗透液进入渗透液罐7，并由渗透液泵9泵送至污水处理站。渗透液冷凝器6中的不凝气在真空机组8的抽吸下进入尾气冷凝器10进行冷凝，得到的冷凝液进入尾冷罐11，不凝气则经不凝尾气管排放至尾气总管，而尾冷罐11内的冷凝液被泵送至污水处理站。During operation, the ethanol vapor extracted from the top outlet of the ethanol refining tower 1 is condensed to obtain a low-concentration ethanol solution (the ethanol purity of the low-concentration ethanol solution is about 95%), and part of the low-concentration ethanol solution enters the raw material storage tank 2. The low-concentration ethanol solution in the raw material storage tank 2 enters the preheater 4, and then enters the evaporator 5, absorbs heat in the evaporator 5 and is converted into raw material steam, and then the raw material steam enters the two membrane separation units 3 in parallel. Under the suction of the vacuum unit 8, the steam partial pressure difference between the upstream side and the downstream side of the membrane module causes the water content and a small amount of alcohols such as ethanol in the raw material steam to permeate from the upstream side of the membrane to the downstream side of the membrane through the membrane module, and the upstream side of the last stage of the membrane module obtains a mixed alcohol vapor with a water content of ≤0.3wt%, and the permeate vapor on the downstream side of the membrane enters the permeate condenser 6, and the condensed permeate enters the permeate tank 7, and is pumped to the sewage treatment station by the permeate pump 9. The non-condensable gas in the permeate condenser 6 enters the tail gas condenser 10 for condensation under the suction of the vacuum unit 8, and the obtained condensate enters the tail cooling tank 11, and the non-condensable gas is discharged to the tail gas main pipe through the non-condensable tail gas pipe, and the condensate in the tail cooling tank 11 is pumped to the sewage treatment station.
含水量≤0.3wt％的混合醇蒸汽进入预热器4内，与预热器4内的低浓度乙醇溶液换热，使得低浓度乙醇溶液的温度上升，减少低浓度乙醇溶液在蒸发器5时蒸发所需的蒸汽量，从而实现混合醇蒸汽热量的回收利用，避免能源浪费。混合醇蒸汽在预热器4内降温后进入精馏塔12，精馏塔12设计采用高效规整填料，塔釜采用热虹吸式再沸器，自然循环。在常压加热条件下，精馏塔12塔顶出口采出含甲醇的乙醇蒸汽，塔顶蒸汽经一级冷凝器13和二级冷凝器14冷凝后进入冷凝液储罐15，冷凝液储罐15内的冷凝液部分回流至精馏塔12塔顶，另一部分被泵送至乙醇脱轻塔16，以便进一步分离甲醇和乙醇，从而实现甲醇的分离回收。The mixed alcohol steam with a water content of ≤0.3wt% enters the preheater 4 and exchanges heat with the low-concentration ethanol solution in the preheater 4, so that the temperature of the low-concentration ethanol solution rises, and the amount of steam required for the low-concentration ethanol solution to evaporate in the evaporator 5 is reduced, thereby realizing the recycling of the heat of the mixed alcohol steam and avoiding energy waste. After cooling in the preheater 4, the mixed alcohol steam enters the distillation tower 12, which is designed with high-efficiency structured packing, and the tower bottom adopts a thermal siphon reboiler for natural circulation. Under normal pressure heating conditions, the top outlet of the distillation tower 12 extracts ethanol steam containing methanol, and the top steam enters the condensate storage tank 15 after being condensed by the primary condenser 13 and the secondary condenser 14. The condensate in the condensate storage tank 15 is partially refluxed to the top of the distillation tower 12, and the other part is pumped to the ethanol light removal tower 16 to further separate methanol and ethanol, thereby realizing the separation and recovery of methanol.
精馏塔12塔釜出口采出乙醇成品，经乙醇冷凝器18冷凝后，检测乙醇的纯度，当乙醇的纯度达标(乙醇纯度≥99.5％)时，乙醇成品被泵送至乙醇成品储罐17内存放；当乙醇的纯度未达标时，乙醇被泵送至乙醇精制塔1或者原料储罐2，以便其重新进入纯化过程。The finished ethanol product is taken out from the outlet of the bottom of the distillation tower 12, and after condensation in the ethanol condenser 18, the purity of the ethanol is tested. When the purity of the ethanol meets the standard (ethanol purity ≥ 99.5%), the finished ethanol product is pumped to the finished ethanol product storage tank 17 for storage; when the purity of the ethanol does not meet the standard, the ethanol is pumped to the ethanol refining tower 1 or the raw material storage tank 2 so that it can re-enter the purification process.
实施例二Embodiment 2
本实施例与实施例一的区别之处在于：如图3所示，本实施例中，精馏塔12与乙醇成品储罐17之间设有中间罐19，中间罐19的数量为两个以上，两个以上的中间罐19并联设置，中间罐19与乙醇成品储罐17连接，且中间罐19与乙醇成品储罐17之间设有阀门Ⅰ和乙醇成品泵20，中间罐19与原料储罐2连接，且中间罐19与原料储罐2之间设有阀门Ⅱ和乙醇回料泵21。更为具体地，中间罐19的数量为两个。The difference between this embodiment and the first embodiment is that, as shown in FIG3 , in this embodiment, an intermediate tank 19 is provided between the distillation tower 12 and the ethanol product storage tank 17, the number of the intermediate tanks 19 is more than two, the more than two intermediate tanks 19 are arranged in parallel, the intermediate tank 19 is connected to the ethanol product storage tank 17, and a valve I and an ethanol product pump 20 are provided between the intermediate tank 19 and the ethanol product storage tank 17, the intermediate tank 19 is connected to the raw material storage tank 2, and a valve II and an ethanol return pump 21 are provided between the intermediate tank 19 and the raw material storage tank 2. More specifically, the number of the intermediate tanks 19 is two.
本实施例中，当乙醇纯度未达标，但乙醇出路未及时切换时，将会导致纯度未达标的乙醇进入乙醇成品储罐17的路线内，此时，中间罐19的设计则能够暂时存放这些纯度未达标的乙醇，从而避免未达标的乙醇直接进入乙醇成品储罐17而影响乙醇成品储罐17内的乙醇品质。另外，并联设置的中间罐19，能够在上一中间罐19装满后使用下一中间罐19。当中间罐19内的乙醇装满时，检测中间罐19内乙醇的纯度，若纯度达标，则中间罐19内的乙醇通过乙醇成品泵20泵入乙醇成品储罐17内；若纯度不达标，则中间罐19内的乙醇通过乙醇回料泵21泵入原料储罐2，以便乙醇重新进入脱水纯化过程。而且，中间罐19内的乙醇通过乙醇回料泵21泵入原料储罐2部分后，中间罐19内的乙醇液位下降，后续精馏塔12塔釜出口采出的乙醇产品(纯度≥99.5％，且纯度有可能达到99.9％)进入该中间罐19内，与罐内纯度不达标的乙醇混合，使得中间罐19内的乙醇纯度达标，即，通过置换手段使得中间罐19内的乙醇纯度达标。In this embodiment, when the purity of ethanol does not meet the standard, but the ethanol outlet is not switched in time, the ethanol with unqualified purity will enter the route of the ethanol finished product storage tank 17. At this time, the design of the intermediate tank 19 can temporarily store the ethanol with unqualified purity, thereby preventing the ethanol with unqualified purity from directly entering the ethanol finished product storage tank 17 and affecting the quality of the ethanol in the ethanol finished product storage tank 17. In addition, the intermediate tanks 19 arranged in parallel can use the next intermediate tank 19 after the previous intermediate tank 19 is full. When the ethanol in the intermediate tank 19 is full, the purity of the ethanol in the intermediate tank 19 is detected. If the purity meets the standard, the ethanol in the intermediate tank 19 is pumped into the ethanol finished product storage tank 17 through the ethanol finished product pump 20; if the purity does not meet the standard, the ethanol in the intermediate tank 19 is pumped into the raw material storage tank 2 through the ethanol return pump 21, so that the ethanol re-enters the dehydration purification process. Moreover, after the ethanol in the intermediate tank 19 is pumped into the raw material storage tank 2 by the ethanol return pump 21, the ethanol liquid level in the intermediate tank 19 drops, and the ethanol product (purity ≥ 99.5%, and the purity may reach 99.9%) extracted from the bottom outlet of the subsequent distillation tower 12 enters the intermediate tank 19 and mixes with the ethanol in the tank that does not meet the purity standard, so that the ethanol purity in the intermediate tank 19 meets the standard, that is, the ethanol purity in the intermediate tank 19 meets the standard through replacement means.
以上所述的仅是本实用新型的实施例，方案中公知的具体结构及特性等常识在此未作过多描述。应当指出，对于本领域的技术人员来说，在不脱离本实用新型结构的前提下，还可以作出若干变形和改进，这些也应该视为本实用新型的保护范围，这些都不会影响本实用新型实施的效果和本实用新型的实用性。说明书中的具体实施方式等记载可以用于解释权利要求的内容。The above is only an embodiment of the utility model, and the common knowledge such as the known specific structure and characteristics in the scheme is not described in detail here. It should be pointed out that for those skilled in the art, several deformations and improvements can be made without departing from the structure of the utility model, which should also be regarded as the protection scope of the utility model, and these will not affect the effect of the implementation of the utility model and the practicality of the utility model. The specific implementation methods and other records in the specification can be used to explain the content of the claims.
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