CN106866368A - 基于气提法和真空膜蒸馏法的气田含醇污水甲醇回收装置及工艺 - Google Patents
基于气提法和真空膜蒸馏法的气田含醇污水甲醇回收装置及工艺 Download PDFInfo
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- CN106866368A CN106866368A CN201710041388.3A CN201710041388A CN106866368A CN 106866368 A CN106866368 A CN 106866368A CN 201710041388 A CN201710041388 A CN 201710041388A CN 106866368 A CN106866368 A CN 106866368A
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- methanol
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- OKKJLVBELUTLKV-UHFFFAOYSA-N methanol Chemical compound data:image/svg+xml;base64,PD94bWwgdmVyc2lvbj0nMS4wJyBlbmNvZGluZz0naXNvLTg4NTktMSc/Pgo8c3ZnIHZlcnNpb249JzEuMScgYmFzZVByb2ZpbGU9J2Z1bGwnCiAgICAgICAgICAgICAgeG1sbnM9J2h0dHA6Ly93d3cudzMub3JnLzIwMDAvc3ZnJwogICAgICAgICAgICAgICAgICAgICAgeG1sbnM6cmRraXQ9J2h0dHA6Ly93d3cucmRraXQub3JnL3htbCcKICAgICAgICAgICAgICAgICAgICAgIHhtbG5zOnhsaW5rPSdodHRwOi8vd3d3LnczLm9yZy8xOTk5L3hsaW5rJwogICAgICAgICAgICAgICAgICB4bWw6c3BhY2U9J3ByZXNlcnZlJwp3aWR0aD0nMzAwcHgnIGhlaWdodD0nMzAwcHgnIHZpZXdCb3g9JzAgMCAzMDAgMzAwJz4KPCEtLSBFTkQgT0YgSEVBREVSIC0tPgo8cmVjdCBzdHlsZT0nb3BhY2l0eToxLjA7ZmlsbDojRkZGRkZGO3N0cm9rZTpub25lJyB3aWR0aD0nMzAwLjAnIGhlaWdodD0nMzAwLjAnIHg9JzAuMCcgeT0nMC4wJz4gPC9yZWN0Pgo8cGF0aCBjbGFzcz0nYm9uZC0wIGF0b20tMCBhdG9tLTEnIGQ9J00gMTc3LjAsMTUwLjAgTCAxMDMuOCwxNTAuMCcgc3R5bGU9J2ZpbGw6bm9uZTtmaWxsLXJ1bGU6ZXZlbm9kZDtzdHJva2U6I0U4NDIzNTtzdHJva2Utd2lkdGg6Mi4wcHg7c3Ryb2tlLWxpbmVjYXA6YnV0dDtzdHJva2UtbGluZWpvaW46bWl0ZXI7c3Ryb2tlLW9wYWNpdHk6MScgLz4KPHBhdGggY2xhc3M9J2JvbmQtMCBhdG9tLTAgYXRvbS0xJyBkPSdNIDEwMy44LDE1MC4wIEwgMzAuNSwxNTAuMCcgc3R5bGU9J2ZpbGw6bm9uZTtmaWxsLXJ1bGU6ZXZlbm9kZDtzdHJva2U6IzNCNDE0MztzdHJva2Utd2lkdGg6Mi4wcHg7c3Ryb2tlLWxpbmVjYXA6YnV0dDtzdHJva2UtbGluZWpvaW46bWl0ZXI7c3Ryb2tlLW9wYWNpdHk6MScgLz4KPHRleHQgeD0nMjIzLjEnIHk9JzE3MC4wJyBjbGFzcz0nYXRvbS0wJyBzdHlsZT0nZm9udC1zaXplOjQwcHg7Zm9udC1zdHlsZTpub3JtYWw7Zm9udC13ZWlnaHQ6bm9ybWFsO2ZpbGwtb3BhY2l0eToxO3N0cm9rZTpub25lO2ZvbnQtZmFtaWx5OnNhbnMtc2VyaWY7dGV4dC1hbmNob3I6c3RhcnQ7ZmlsbDojRTg0MjM1JyA+TzwvdGV4dD4KPHRleHQgeD0nMjUwLjcnIHk9JzE3MC4wJyBjbGFzcz0nYXRvbS0wJyBzdHlsZT0nZm9udC1zaXplOjQwcHg7Zm9udC1zdHlsZTpub3JtYWw7Zm9udC13ZWlnaHQ6bm9ybWFsO2ZpbGwtb3BhY2l0eToxO3N0cm9rZTpub25lO2ZvbnQtZmFtaWx5OnNhbnMtc2VyaWY7dGV4dC1hbmNob3I6c3RhcnQ7ZmlsbDojRTg0MjM1JyA+SDwvdGV4dD4KPC9zdmc+Cg== data:image/svg+xml;base64,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 OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 288
- 239000012528 membrane Substances 0.000 title claims abstract description 90
- 238000000034 method Methods 0.000 title claims abstract description 50
- 239000010865 sewage Substances 0.000 title claims abstract description 47
- 238000004821 distillation Methods 0.000 title claims abstract description 46
- 238000011084 recovery Methods 0.000 title claims abstract description 39
- 230000001476 alcoholic Effects 0.000 title claims abstract description 25
- 238000000605 extraction Methods 0.000 title claims abstract description 23
- 239000007789 gas Substances 0.000 claims abstract description 90
- 239000007788 liquid Substances 0.000 claims abstract description 36
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances data:image/svg+xml;base64,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 data:image/svg+xml;base64,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 O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 31
- 239000002994 raw material Substances 0.000 claims abstract description 17
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N ethanol Chemical compound data:image/svg+xml;base64,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 data:image/svg+xml;base64,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 CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 13
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O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 239000002033 PVDF binder Substances 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- WVDDGKGOMKODPV-UHFFFAOYSA-N benzyl alcohol Chemical compound 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OCC1=CC=CC=C1 WVDDGKGOMKODPV-UHFFFAOYSA-N 0.000 description 1
- 229960004217 benzyl alcohol Drugs 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000005039 chemical industry Methods 0.000 description 1
- 230000001934 delay Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 230000003628 erosive Effects 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000005755 formation reaction Methods 0.000 description 1
- 150000004677 hydrates Chemical class 0.000 description 1
- 230000002209 hydrophobic Effects 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/447—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by membrane distillation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/32—Hydrocarbons, e.g. oil
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Abstract
本发明涉及一种基于气提法和真空膜蒸馏法的气田含醇污水甲醇回收装置及工艺，采用先气提得到含杂质较少的稀甲醇溶液后采用真空膜蒸馏对稀甲醇溶液进行提浓的复合工艺路线。本发明的有益效果是：不需要复杂的精馏塔、重沸器、回流罐等相关设备，大大减少了设备投资；该集成工艺无甲醇回流液，避免了回流液和塔底残液的重复加热，充分利用甲醇产品、塔底水余热加热原料，气提段加热原料的余热又为真空膜蒸馏的相变提供了能量，大大降低了甲醇回收能耗，提高了经济效益；避免了原料含醇污水杂质含量较高，溶液污染疏水微孔膜的问题，延长了膜的使用寿命；集成应用了气提、真空膜蒸馏复合工艺，提高了回收效率，降低了含醇污水的甲醇含量。
Description
基于气提法和真空膜蒸馏法的气田含醇污水甲醇回收装置及 工艺
技术领域
[0001] 本发明属于污水处理工艺及节能技术领域，涉及一种基于气提法和真空膜蒸馏法 的气田含醇污水甲醇回收装置及工艺。
背景技术
[0002] 在天然气生产中，天然气水合物常常造成管道、阀门和设备等的堵塞，为抑制水合 物的形成，通常由采气井口向集输管道中注入水合物抑制剂。甲醇是气田生产中较常用的 抑制剂。由井口注入管道的甲醇，在集气站伴随天然气脱水分离，产生了气田含醇污水。天 然气开采中，由于注醇量大，如不回收，甲醇的耗资较大，另外甲醇属于毒性物质，污水直接 排放会造成环境污染等问题，给气田的生产和运行带来很大的影响。因此，污水中甲醇必须 回收循环使用，达到注入-回收-再注入的良性循环，降低天然气生产成本，减少对环境的污 染。
[0003] 含甲醇水溶液的回收处理方法包括吸附、精馏、萃取等，当甲醇浓度较高时，可采 用精馏、萃取法，当其浓度较低时宜采用吸附法。精馏法通常应用于有机物含量在5〜 10wt%的浓度范围内、萃取法通常应用于有机物含量在1〜10wt%的浓度范围内，吸附法通 常应用于有机物含量小于O.lwt%的浓度范围下。吸附法对水溶液的处理是一种重要和成 熟的技术，活性碳是广泛采用的吸附剂。吸附系统包括颗粒活性炭吸附柱，以及饱和活性炭 的热再生装置。当饱和活性炭加热再生时，某些甲醇会在再生温度范围内分解，通常该法应 用于甲醇低浓度场合，如1 •〇 x l〇_4kg/kg以下，当甲醇的浓度高于1.0 X l〇_3kg/kg时，活性 炭的需用量非常大，两且再生将会很频繁。
[0004] 目前，国内外气田处理含醇污水工艺流程归纳起来大多数采用3段处理工艺，即除 油、混凝沉降（或气浮）、过滤，再辅以阻垢、缓蚀、杀菌处理后进入精馏塔回收甲醇。精馏法 仍然是最常用的甲醇回收方法，但总体来看，精馏法甲醇回收工艺，投资大，能耗高，精镏塔 内填料易堵塞，设备结垢、腐蚀严重。因此，有必要开发新型含甲醇水溶液的回收处理工艺， 降低甲醇回收能耗，实现气田含醇污水处理的经济性和环保性双赢。
[0005] 同时上述技术虽均可以回收处理水中有机污染物，但没有一种技术可以解决整个 浓度范围内的问题，不同的技术对不同体系的处理性能也不相同。而膜蒸馏技术处理的有 机物浓度范围比上述技术要广的多。目前国内大多数气田产出水中甲醇含量为5〜20%，最 低可至1 %左右，其变化幅度之大是一般化工精馏过程难以遇到的，而膜蒸馏技术具有的处 理有机物浓度范围广的特点正好可以解决该难题。且膜蒸馏处理含醇污水流程简单，膜组 件简洁紧凑，易于自动化操作，维护方便，无二次污染，可使用低品位能源，进料温度远低于 常规精馏工艺。甲醇气提工艺是利用甲醇沸点低，在醇水溶液中分压高的特性，在经过特殊 设计的气提器内，利用极性络合物的特性将甲醇与水分离，具有流程短、易于操作等特点， 可实现气田含醇污水处理过程中甲醇的初步分离，从而得到浓度较低的稀甲醇溶液，然后 再利用真空膜蒸馏法进行甲醇溶液的浓缩。因此基于气提法和真空膜蒸馏法的甲醇回收工 艺对于气田含醇污水甲醇再生问题而言是一种十分有前途的新工艺。
[0006] 根据本发明技术特点检索了国内外数据库，发现在国内外采用精馏法进行气田含 醇污水甲醇回收的专利和报道较多，但未见采用气提法和真空膜蒸馏法集成工艺的气田含 醇污水甲醇回收装置及工艺相关专利和报道。有专利申请号：201220129330.7—种二甲醚 气化塔残液中甲醇回收装置，该实用新型公开了一种二甲醚气化塔残液中甲醇回收装置， 包括气提塔体。气提塔体下端内安装有盘管，盘管连接到气提塔体侧边的残液入口，二甲醚 生产残液进入气提塔，经塔内盘管加热变成气体，由塔顶导出进入冷凝器冷凝分离后得到 甲醇含量为60-80%的回收液，冷凝器出液管分为两根管道，一根为回流管，连接到气提塔 体上端，另一根为采出管，连接到二甲醚生产系统回收液。因此该专利采用的是残液通过盘 管加热后形成的含醇气体作为气提气，同塔顶冷凝回流液进行气液交换后完成甲醇溶液的 提浓回收。专利申请号:201010290311 • 8—种水中挥发性醇类有机物的去除和回收方法，该 发明专利发明的方法是在进料侧废水中混入一定比例的气体，气液共同连续进入真空膜蒸 馏组件，渗透侧抽真空，废水中的气体、水蒸气以及有机物蒸汽透过膜孔在渗透侧冷凝，为 一种气提式的真空膜蒸馏过程。本发明采用的则是先气提后真空膜蒸馏的集成工艺进行含 醇污水的甲醇回收，其中气提工艺采用空气或气田所产天然气作为气提气，气提工艺过程 也不存在回流液。因此本发明的工艺路线和原理都不同于上述发明专利。
发明内容
[0007] 本发明要解决的技术问题是:基于上述问题，本发明提供一种具有更高的分离效 率、操作更简便、能耗更小、更易产业化的气田含醇污水甲醇回收集成新工艺，以解决甲醇 回收工艺对原料污水甲醇含量大幅度变化的适应问题，且降低甲醇回收能耗，实现气田含 醇污水处理的经济性和环保性双赢。
[0008]本发明解决其技术问题所采用的一个技术方案是:基于气提法和真空膜蒸馏法的 气田含醇污水甲醇回收装置，包括气提工艺段装置和真空膜蒸馏段装置。
[0009]气提工艺段装置包括气提塔，气提塔的上入口依次管路连接有加热换热器、精细 过滤器、原料-塔底水换热器、原料-甲醇产品换热器、原料栗，气提塔的上部出口依次管路 连接有原料-甲醇产品换热器、气液分离器，气提塔的下出口依次管路连接有原料—塔底水 换热器、外排储罐，气提塔的下部进口管路连接有空气压缩机，气液分离器的上部出口连通 气提塔的下部进口，气液分离器的下部出口管路连接有稀甲醇储罐；
[0010]真空膜蒸馏段装置包括膜分离器，膜分离器的管程入口管路连接有稀溶液中间缓 冲罐，稀溶液中间缓冲罐的入口与稀甲醇储罐出口连通，膜分离器的冷侧出口依次管路连 接有真空冷凝室、甲醇产品储罐、真空泵，膜分离器的热侧出口与稀溶液中间缓冲罐的入口 连通，稀溶液中间缓冲罐的另一个输出端与外排储罐输入端连通。
[001进一步地，气提塔的下部出口与原料-塔底水换热器之间的管路上设有塔底泵，气 液分离器的上部出口与气提塔的下部进口之间的管路上设有电动阀〗，稀溶液中间缓冲罐 的入口与稀甲醇储罐出口之间的管路上设有电动阀n，膜分离器的热侧出口与稀溶液中间 缓冲罐的入口之间的管路上设有电动阀m，膜分离器的管程入口与稀溶液中间缓冲罐入口 之间的管路上设有泵，稀溶液中间缓冲罐与外排储罐之间的连接管路上设有电动阀jv。 [0012]进一步地，空气压缩机采用干空气或产自气田经过脱水脱硫脱凝析液处理的千天 然气。
[0013] 进一步地，稀溶液中间缓冲罐设有电加热装置。
[0014] 进一步地，膜分离器采用中空纤维膜组件，膜材料采用聚四氟乙烯膜。
[0015] 采用基于气提法和真空膜蒸馏法的气田含醇污水甲醇回收装置的回收工艺，包括 气提工艺段和真空膜蒸馏段，具体为：
[0016] 气提工艺段:经过预处理的含醇污水由原料泵加压后，进入原料-甲醇产品换热器 进行预热，然后再进入原料-塔底水换热器进一步预热，而后经精细过滤器过滤后进入加热 换热器，由气提塔上部进口进入气体塔，来自空气压缩机的干气体从气提塔下部的进口进 入气提塔;气提塔内液相自上而下流动与从下而上移动的干空气逆流接触，完成传质传热 过程;含有甲醇蒸气和部分水蒸气的气体从气提塔顶部出口进入原料-甲醇产品换热器换 热，然后进入气液分离器，在气液分离器中，甲醇蒸汽和水蒸气冷凝成稀甲醇溶液从分离器 底部分出进入稀甲醇储罐，气提空气从气液分离器顶部分出返回到气提塔下部进口重新作 为气提气;流入气提塔塔底的脱甲醇废水进入原料-塔底水换热器换热，后进入外排储罐， 而后回注地层；
[0017] 真空膜蒸镏段:来自稀甲醇储罐的稀甲醇溶液进入稀溶液中间缓冲罐，而后送入 膜分离器管程，甲醇在膜表面汽化，沿膜微孔向真空冷凝室扩散，经过真空冷凝室冷凝后进 入甲醇产品储罐，少量的不凝物通过真空泵排除，截留在热侧的水分由膜分离器热侧出口 返回到稀溶液中间缓冲罐循环提浓，当稀溶液中间缓冲罐中的甲醇溶液浓度达到可外排浓 度要求后，将该溶液排往外排储罐，然后再次接收来自稀甲醇储罐的稀甲醇溶液进行下一 次循环提浓。
[0018] 进一步地，空气压缩机采用干空气或产自气田经过脱水脱硫脱凝析液处理的千天 然气。
[0019] 进一步地，稀溶液中间缓冲罐设有电加热装置。
[0020] 进一步地，膜分离器采用中空纤维膜组件，膜材料采用聚四氟乙烯膜。
[0021]本发明的有益效果是：（1)甲醇气提工艺利用了甲醇沸点低，在醇水溶液中分压高 的特性，在经过特殊设计的气提器内，利用极性络合物的特性将甲醇与水分离，具有流程 短、易于操作等特点。同时真空膜蒸馏法处理含醇污水流程简单，膜组件简洁紧凑，易于自 动化操作，维护方便，无二次污染。因此，两种方法集成的甲醇回收工艺同传统的精馏法回 收工艺相比较，不需要复杂的精馏塔、重沸器、回流罐等相关设备，大大减少了设备投资； [0022] (2)该集成工艺气提段进口温度低于传统精馏法精馏塔塔底含醇污水温度，且没 有回流液，避免了回流液和塔底残液的重复加热，气提工艺段采用了原料-甲醇产品换热 器、原料-塔底水换热器各一具，充分利用甲醇产品、塔底水余热加热原料，大大降低外热源 的消耗量，同时实现了原料的加热与甲醇初产品的冷却，达到输送及后续真空膜蒸馏处理 工艺的温度要求;同时真空膜蒸馏是一个有相变的膜过程，汽化潜热降低了热能的利用率， 与其他膜过程相比，膜蒸馏在有廉价能源可利用的情况下才更有实用意义，真空膜蒸馏工 艺同气提工艺结合，可充分回收利用气提段加热含醇原料的热量，因此该集成工艺大大减 少了甲醇回收能耗，提高了经济效益；
[0023] (3)真空膜蒸馏过程采用疏水微孔膜，为了保证膜处理效果的稳定性，降低膜的维 护次数，延长使用寿命，需要对料液进行必要的预处理;虽然气田含醇污水通过预处理装置 进行了预处理但由于预处理工艺和装置的局限性，原料液中还含有少量的凝析油、污泥和 浮渣且矿化度较高，容易堵塞疏水微孔膜，造成对中空纤维膜的污染。因此如果直接采用真 空膜蒸馈法处理气田含醇污水，将大大降低处理效率。而采用先气提再真空膜蒸馏的集成 工艺巧妙的解决了该问题。由于气提出来的溶液主要成分是甲醇和水，杂质含量极少，不会 污染疏水微孔膜，因此大大降低了膜的维护次数，延长了膜的使用寿命；
[0024] (4)本发明集成应用了气提、真空膜蒸馏复合工艺，提高了回收效率，降低了含醇 污水的甲醇含量。
附图说明
[0025] 下面结合附图对本发明进一步说明。
[0026]图1是本发明的结构示意图；
[0027]其中：1 •原料泵，2 •原料-甲醇产品换热器，3 •原料-塔底水换热器，4.精细过滤器， 5.加热换热器，6.气提塔，7.空气压缩机，8.气液分离器，9.稀甲醇储罐，10.电动阀I，11.塔 底泵，I2•外排储罐，I3•电动阀II，14.稀溶液中间缓冲罐，15.杲，16.膜分离器，17.真空冷 凝室，18 •甲醇产品储罐，19 •真空泵，20 •电动阀IE，21.电动阀IV。
具体实施方式
[0028] 现在结合具体实施例对本发明作进一步说明，以下实施例旨在说明本发明而不是 对本发明的进一步限定。
[0029] 如图1所示的基于气提法和真空膜蒸馏法的气田含醇污水甲醇回收装置，包括气 提工艺段装置和真空膜蒸馏段装置，
[0030]气提工艺段装置包括气提塔6,气提塔6的上入口依次管路连接有加热换热器5、精 细过滤器4、原料-塔底水换热器3、原料-甲醇产品换热器2、原料泵1，气提塔6的上部出口依 次管路连接有原料-甲醇产品换热器2、气液分离器8，气提塔6的下出口依次管路连接有原 料-塔底水换热器3、外排储罐12，气提塔6的下部进口管路连接有空气压缩机7，气液分离器 8的上部出口连通气提塔6的下部进口，气液分离器8的下部出口管路连接有稀甲醇储罐9; [0031]真空膜蒸馏段装置包括膜分离器I6,膜分离器16的管程入口管路连接有稀溶液中 间缓冲罐14，稀溶液中间缓冲罐14的入口与稀甲醇储罐9出口连通，膜分离器16的冷侧出口 依次管路连接有真空冷凝室17、甲醇产品储罐18、真空栗19，膜分离器16的热侧出口与稀溶 液中间缓冲罐14的入口连通，稀溶液中间缓冲罐14的另一个输出端与外排储罐12输入端连 通。
[0032]气提塔6的下部出口与原料-塔底水换热器3之间的管路上设有塔底泵H，气液分 离器8的上部出口与气提塔6的下部进口之间的管路上设有电动阀110,稀溶液中间缓冲罐 14的入口与稀甲醇储罐9出口之间的管路上设有电动阀II13,膜分离器16的热侧出口与稀 溶液中间缓冲罐14的入口之间的管路上设有电动阀m20,膜分离器16的管程入口与稀溶液 中间缓冲罐14入口之间的管路上设有泵15，稀溶液中间缓冲罐14与外排储罐12之间的连接 管路上设有电动阀IV21。
[0033] 空气压缩机7采用干空气或产自气田经过脱水脱硫脱凝析液处理的干天然气。 [0034] 稀溶液中间缓冲罐14设有电加热装置，当稀溶液中间缓冲罐14中的甲醇溶液温度 不足40〜45 °c时，电加热装置将自动启动，使罐内溶液保持40〜45 °C。
[0035]^膜分离器16采用中空纤维膜组件，膜材料采用聚四氟乙烯膜。聚四氟乙烯膜在各 种操作条件下分离因子均高于聚偏氟乙烯膜，因此为了回收到高浓度的甲醇，聚四氟 乙稀膜更适合膜蒸馏法提浓甲醇废水。真空设备可为滑片式、旋片式真空栗，或其他适合抽 真空的动力设备。
[0036]气提塔6属于填料塔的一种，在气提塔中装有一定高度的填料层，该填料多选用波 纹填料，因为波纹料具有压降小、生产能力大、效率高、操作弹性大的特点。
[0037]气田含醇污水经过预处理装置进行处理完成除油、PH值调整、氧化除铁、混凝沉降 等预处理工艺，以保证含醇污水水质的稳定性，以减少污水对后续甲醇回收系统设备的腐 蚀、结垢、堵塞。基于气提法和真空膜蒸馈法的气田含醇污水甲醇回收装置的回收工艺包括 气提工艺段和真空膜蒸馏段，具体为：
[^038]经过预处理的含醇污水由原料泵1加压后，进入原料-甲醇产品换热器2，利用甲醇 产品对原料进行预热，然后再进入原料-塔底水换热器3利用塔底废水进一步预热原料，而 后经精细过滤器4过滤后进入加热换热器5利用蒸汽将原料水加热到90〜95°C，由气提塔6 上部的进口进入气体塔6,来自空气压缩机7的干空气从气提塔6下部的进口进入气提塔6; 气提塔6内液相自上而下流动与从下而上移动的干空气逆流接触，完成传质传热过程；由于 甲醇挥发性高，干空气与温度较高的甲醇水溶液接触过程中，可以将水溶液中的甲醇气提 出来，含有甲醇蒸气和部分水蒸气的气体气从气提塔6顶部出口进入原料-甲醇产品换热器 2同原料含醇污水换热降温到40〜45°C，然后进入气液分离器8,在气液分离器8中，甲醇蒸 汽和水蒸气冷凝成稀甲醇溶液从气液分离器8底部分出进入稀甲醇储罐9，气提空气从气液 分离器8顶部分出经过电动阀110返回到气提塔6气体入口重新作为气提气;流入气提塔6塔 底的脱甲醇废水，用塔底泵11抽出进入原料-塔底水换热器3中同原料甲醇污水换热至40°C 以下后进入外排储罐12，而后回注地层。
[0039] 来自稀甲醇储罐9的40〜45°C稀甲醇溶液通过电动阀n 13进入稀溶液中间缓冲罐 14,稀溶液中间缓冲罐14中的甲醇稀溶液由栗15送入膜分离器16管程，由于膜是疏水膜，水 不会从膜孔中通过，被截留在热侧，甲醇在膜表面汽化，在膜两侧蒸汽压差的推动下，遵循 亨利定律，沿膜微孔向真空冷凝室17扩散，进入真空冷凝室17的甲醇蒸汽立即由连接在甲 醇产品储罐18上的真空泵19抽走，冷凝室保持8〜10kPa的真空度，采用循环水冷却，冷却温 度为l〇°C，使膜两侧始终存在着一个较大甲醇蒸汽压差，稀甲醇溶液中的甲醇就源源不断 的被提取出来，经过冷凝室17冷凝后进入甲醇产品储罐18,少量的不凝物通过真空泵19排 除，截留在热侧的水分由膜分离器热侧出口经过电动阀HI20返回到稀溶液中间缓冲罐14循 环提浓，当稀溶液中间缓冲罐14中的甲醇溶液浓度达到可外排浓度要求后，通过电动阀IV 21将该溶液排往外排储罐12,然后再次接收来自稀甲醇储罐9的稀甲醇溶液进行下一次循 环提浓。
[0040] 以上述依据本发明的理想实施例为启示，通过上述的说明内容，相关工作人员完 全可以在不偏离本项发明技术思想的范围内，进行多样的变更以及修改。本项发明的技术 性范围并不局限于说明书上的内容，必须要根据权利要求范围来确定其技术性范围。
Claims (9)
1.基于气提法和真空膜蒸馏法的气田含醇污水甲醇回收装置，其特征是:包括气提工 艺段装置和真空膜蒸馏段装置， 气提工艺段装置包括气提塔(6)，气提塔(6)的上入口依次管路连接有加热换热器(5)、 精细过滤器(4)、原料-塔底水换热器(3)、原料-甲醇产品换热器(2)、原料泵(1)，气提塔(6) 的上部出口依次管路连接有原料-甲醇产品换热器(2)、气液分离器(8)，气提塔⑹的下出 口依次管路连接有原料-塔底水换热器(3)、外排储罐(12)，气提塔⑹的下部进口管路连接 有空气压缩机(7)，气液分离器(8)的上部出口连通气提塔⑹的下部进口，气液分离器(8) 的下部出口管路连接有稀甲醇储罐(9); 真空膜蒸馏段装置包括膜分离器（ie)，膜分离器（16)的管程入口管路连接有稀溶液中 间缓冲罐（14)，稀溶液中间缓冲罐(14)的入口与稀甲醇储罐⑼出口连通，膜分离器（16)的 冷侧出口依次管路连接有真空冷凝室（17)、甲醇产品储罐(18)、真空泵(19)，膜分离器(16) 的热侧出口与稀溶液中间缓冲罐（14)的入口连通，稀溶液中间缓冲罐(14)的另一个输出端 与外排储罐(12)输入端连通。
2. 根据权利要求1所述的基于气提法和真空膜蒸馏法的气田含醇污水甲醇回收装置， 其特征是:所述的气提塔(6)的下部出口与原料-塔底水换热器(3)之间的管路上设有塔底 泵（11)，气液分离器（8)的上部出口与气提塔（6)的下部进口之间的管路上设有电动阀I (1〇)，稀溶液中间缓冲罐（14)的入口与稀甲醇储罐（9)出口之间的管路上设有电动阀n (I3)，膜分离器(16)的热侧出口与稀溶液中间缓冲罐(14)的入口之间的管路上设有电动阀 m (20)，膜分离器（16)的管程入口与稀溶液中间缓冲罐（14)入口之间的管路上设有泵 (15)，稀溶液中间缓冲罐(14)与外排储罐(12)之间的连接管路上设有电动阀IV (21)。
3. 根据权利要求1所述的基于气提法和真空膜蒸馏法的气田含醇污水甲醇回收装置， 其特征是:所述的空气压缩机(7)采用干空气或产自气田经过脱水脱硫脱凝析液处理的干 天然气。
4. 根据权利要求1所述的基于气提法和真空膜蒸馏法的气田含醇污水甲醇回收装置， 其特征是:所述的稀溶液中间缓冲罐(14)设有电加热装置。
5. 根据权利要求1所述的基于气提法和真空膜蒸镏法的气田含醇污水甲醇回收装置， 其特征是:所述的膜分离器(16)采用中空纤维膜组件，膜材料采用聚四氟乙烯膜。
6. 采用权利要求1所述的基于气提法和真空膜蒸馏法的气田含醇污水甲醇回收装置的 回收工艺，其特征是:包括气提工艺段和真空膜蒸馏段，具体为： 气提工艺段:经过预处理的含醇污水由原料泵（1)加压后，进入原料-甲醇产品换热器 (2)进行预热，然后再进入原料-塔底水换热器(3)进一步预热，而后经精细过滤器(4)过滤 后进入加热换热器(5)，由气提塔(6)上部进口进入气体塔(6)，来自空气压缩机(7)的干气 体从气提塔(6)下部的进口进入气提塔;气提塔(6)内液相自上而下流动与从下而上移动的 干空气逆流接触，完成传质传热过程;含有甲醇蒸气和部分水蒸气的气体从气提塔^3)顶部 出口进入原料-甲醇产品换热器(2)换热，然后进入气液分离器⑻，在气液分离器⑻中，甲 醇蒸汽和水蒸气冷凝成稀甲醇溶液从分离器底部分出进入稀甲醇储罐(9)，气提空气从气 液分离器⑻顶部分出返回到气提塔⑹下部进口重新作为气提气;流入气提塔⑹塔底的 脱甲醇废水进入原料-塔底水换热器(3)换热，后进入外排储罐(12)，而后回注地层； 真空膜蒸馏段:来自稀甲醇储罐(9)的稀甲醇溶液进入稀溶液中间缓冲罐（14)，而后送 入膜分离器(ie)管程，甲醇在膜表面汽化，沿膜微孔向真空冷凝室（n)扩散，经过真空冷凝 室（17)冷凝后进入甲醇产品储罐（18)，少量的不凝物通过真空栗（19)排除，截留在热侧的 水分由膜分离器（16)热侧出口返回到稀溶液中间缓冲罐(14)循环提浓，当稀溶液中间缓冲 罐(14)中的甲醇溶液浓度达到可外排浓度要求后，通过电动阀IV (21)将该溶液排往外排储 罐(12)，然后再次接收来自稀甲醇储罐(9)的稀甲醇溶液进行下一次循环提浓。
7. 根据权利要求6所述的基于气提法和真空膜蒸馏法的气田含醇污水甲醇回收工艺， 其特征是:所述的空气压缩机(7)采用千空气或产自气田经过脱水脱硫脱凝析液处理的干 天然气。
8. 根据权利要求6所述的基于气提法和真空膜蒸馏法的气田含醇污水甲醇回收工艺， 其特征是:所述的稀溶液中间缓冲罐(14)设有电加热装置。
9. 根据权利要求6所述的基于气提法和真空膜蒸馏法的气田含醇污水甲醇回收工艺， 其特征是:所述的膜分离器(16)采用中空纤维膜组件，膜材料采用聚四氟乙烯膜。
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