CN106348530A - Treatment method for glycerine concentrated sewage of stearic acid production - Google Patents
Treatment method for glycerine concentrated sewage of stearic acid production Download PDFInfo
- Publication number
- CN106348530A CN106348530A CN201610878610.0A CN201610878610A CN106348530A CN 106348530 A CN106348530 A CN 106348530A CN 201610878610 A CN201610878610 A CN 201610878610A CN 106348530 A CN106348530 A CN 106348530A
- Authority
- CN
- China
- Prior art keywords
- water
- treatment system
- concentrated
- treatment
- stearic acid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 title claims abstract description 101
- 235000011187 glycerol Nutrition 0.000 title claims abstract description 44
- QIQXTHQIDYTFRH-UHFFFAOYSA-N octadecanoic acid Chemical compound CCCCCCCCCCCCCCCCCC(O)=O QIQXTHQIDYTFRH-UHFFFAOYSA-N 0.000 title claims abstract description 35
- 235000021355 Stearic acid Nutrition 0.000 title claims abstract description 34
- OQCDKBAXFALNLD-UHFFFAOYSA-N octadecanoic acid Natural products CCCCCCCC(C)CCCCCCCCC(O)=O OQCDKBAXFALNLD-UHFFFAOYSA-N 0.000 title claims abstract description 34
- 239000008117 stearic acid Substances 0.000 title claims abstract description 33
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 32
- 238000000034 method Methods 0.000 title claims abstract description 19
- 239000010865 sewage Substances 0.000 title description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 88
- 239000013505 freshwater Substances 0.000 claims abstract description 26
- 238000001914 filtration Methods 0.000 claims abstract description 22
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 10
- 229910052799 carbon Inorganic materials 0.000 claims description 8
- 239000000498 cooling water Substances 0.000 claims description 8
- 239000004576 sand Substances 0.000 claims description 5
- 238000005374 membrane filtration Methods 0.000 claims description 4
- 238000001223 reverse osmosis Methods 0.000 claims description 3
- 238000003672 processing method Methods 0.000 claims 6
- 230000007613 environmental effect Effects 0.000 abstract description 4
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- 239000003921 oil Substances 0.000 description 10
- 230000008569 process Effects 0.000 description 9
- 239000012528 membrane Substances 0.000 description 5
- 239000002351 wastewater Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- 239000003344 environmental pollutant Substances 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 230000007062 hydrolysis Effects 0.000 description 3
- 238000006460 hydrolysis reaction Methods 0.000 description 3
- 239000005416 organic matter Substances 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000012141 concentrate Substances 0.000 description 2
- 238000012946 outsourcing Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 239000012459 cleaning agent Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000005446 dissolved organic matter Substances 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 239000012153 distilled water Substances 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 229920001971 elastomer Polymers 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000003925 fat Substances 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- CKQVRZJOMJRTOY-UHFFFAOYSA-N octadecanoic acid;propane-1,2,3-triol Chemical compound OCC(O)CO.CCCCCCCCCCCCCCCCCC(O)=O CKQVRZJOMJRTOY-UHFFFAOYSA-N 0.000 description 1
- 230000036284 oxygen consumption Effects 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000012465 retentate Substances 0.000 description 1
- 150000004671 saturated fatty acids Chemical class 0.000 description 1
- 239000002455 scale inhibitor Substances 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000003911 water pollution Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- 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
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- 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
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
本发明涉及一种硬脂酸生产中甘油浓缩下水的处理方法，针对工业硬脂酸生产中甘油浓缩下水，原水收集池中的甘油浓缩下水依次流经MBR过滤系统、一级RO处理系统和二级RO处理系统，MBR过滤系统的浓水输出端连接有生化处理系统的输入端，MBR过滤系统的淡水输出端与一级RO处理系统的输入端连接，一级RO处理系统的浓水输出端与二级RO处理系统的输入端连接，二级RO处理系统的淡水输出端与一级RO处理系统的输入端连接。本发明的有益效果是：产水水质好，生产过程稳定，处理成本低，绿色环保。
The invention relates to a treatment method for concentrated glycerin offwater in the production of stearic acid. Aiming at the concentrated offwater of glycerin in the production of industrial stearic acid, the concentrated offwater of glycerol in the raw water collection pool flows through the MBR filter system, the primary RO treatment system and the secondary Level RO treatment system, the concentrated water output of the MBR filtration system is connected to the input of the biochemical treatment system, the fresh water output of the MBR filtration system is connected to the input of the primary RO treatment system, and the concentrated water output of the primary RO treatment system It is connected to the input end of the secondary RO treatment system, and the fresh water output end of the secondary RO treatment system is connected to the input end of the primary RO treatment system. The invention has the beneficial effects of good water quality, stable production process, low treatment cost and environmental protection.
Description
技术领域technical field
本发明涉及一种硬脂酸生产中甘油浓缩下水的处理方法。The invention relates to a treatment method for concentrated glycerol off-water in stearic acid production.
背景技术Background technique
硬脂酸(十八烷酸，C18H36O2)是现代工业生产中一种重要的化原料，被广泛应用于塑料、橡胶的合成与加工以及硬脂酸盐的生产，在日用化学、涂料、油田化学等工业领域有着重要的用途。作为一种高级饱和脂肪酸，硬脂酸通常以油脂为原料，经水解、蒸馏/精馏和加氢等环节生产得到。在硬脂酸的生产过程中，油脂水解时副产的甘油会形成稀的甘油水溶液。由于物料特性及产品质量要求，通常需在真空条件下控制较高的温度(甘油浓缩温度239℃)来对甘油水进行浓缩，以满足产品质量要求。硬脂酸生产中甘油浓缩下水主要来自甘油水蒸发浓缩过程排放的蒸出水凝液，并有少量蒸汽伴管凝液。由于真空生产过程中有机组分相对挥发度的影响及易挥发性有机组分的存在，甘油浓缩过程中产生的蒸发废水中会含有一定有机组分，其COD值可高达8000mg/L以上，表观为雾状白浊液，有异味。Stearic acid (octadecanoic acid, C 18 H 36 O 2 ) is an important chemical raw material in modern industrial production. It is widely used in the synthesis and processing of plastics and rubber and the production of stearate. Chemical, paint, oilfield chemistry and other industrial fields have important uses. As a higher saturated fatty acid, stearic acid is usually produced from fats and oils through hydrolysis, distillation/rectification and hydrogenation. In the production process of stearic acid, the by-produced glycerol during the hydrolysis of oil will form a dilute glycerin aqueous solution. Due to material characteristics and product quality requirements, it is usually necessary to control higher temperature (glycerin concentration temperature 239°C) under vacuum conditions to concentrate glycerin water to meet product quality requirements. Glycerin concentrated waste water in the production of stearic acid mainly comes from the distilled water condensate discharged during the evaporation and concentration of glycerin water, and a small amount of steam accompanying the condensate. Due to the influence of the relative volatility of organic components in the vacuum production process and the existence of volatile organic components, the evaporation wastewater generated in the glycerin concentration process will contain certain organic components, and its COD value can be as high as 8000mg/L or more. Appears as foggy white turbid liquid with peculiar smell.
我国近年来环境问题日趋突出，水污染尚未得到有效控制。由于甘油浓缩下水中作为活性污泥营养源的有机组分相对单一，常规生化处理效果的稳定性较差，产水会发生较大波动，不能达到排放标准。在目前的生化处理设施中，甘油浓缩废水经厌氧、耗氧处理后，虽然出水COD值最低可降至200mg/L以下，但COD值经常发生持续超标(>500mg/L)，且耗氧处理池中出现污泥膨胀现象，污水不能排放。而转交外协单位处理，由于污水带泥，外协单位拒收，严重影响了企业的正常生产运行。此外，夏季环境温度升高也会加剧污水的异臭味，影响厂区环境。因此，硬脂酸生产中甘油浓缩下水的有效处理具有了重要性和迫切性，甚至污水处理已成为影响企业生产的关键瓶颈。在当前环保问题受到社会的广泛而密切关注的情况下，有效而稳定地处理硬脂酸生产中甘油浓缩下水成为企业需要解决的迫在眉睫的大事。my country's environmental problems have become increasingly prominent in recent years, and water pollution has not been effectively controlled. Since the organic components in the glycerol-concentrated water as the nutrient source of activated sludge are relatively single, the stability of the conventional biochemical treatment effect is poor, and the produced water will fluctuate greatly, which cannot meet the discharge standards. In the current biochemical treatment facilities, after anaerobic and aerobic treatment of concentrated glycerin wastewater, although the COD value of the effluent can be reduced to below 200mg/L, the COD value often continues to exceed the standard (>500mg/L), and the oxygen consumption Sludge bulking occurs in the treatment tank, and sewage cannot be discharged. However, when it was transferred to the outsourcing unit for processing, the outsourcing unit refused to accept it due to the mud in the sewage, which seriously affected the normal production and operation of the enterprise. In addition, the increase in ambient temperature in summer will also aggravate the odor of sewage and affect the environment of the factory area. Therefore, the effective treatment of glycerin concentrated sewage in stearic acid production has become important and urgent, and even sewage treatment has become a key bottleneck affecting the production of enterprises. Under the circumstances that the current environmental protection issues are widely and closely watched by the society, the effective and stable treatment of glycerin concentrated sewage in the production of stearic acid has become an urgent matter for enterprises to solve.
采用精馏分离工艺将导致改造成本及运行成本急剧增高，而使用萃取工艺则还会导致新的污染物引入。活性炭、分子筛等吸附剂对硬脂酸和油脂具有良好的吸附作用，但无法脱除甘油等水溶性较强的污染物。由于过滤精度的限制，溶解态的有机物无法通过常规的板框过滤来脱除，而直接采用可截留分子的膜分离设备，由于废水中含有硬脂酸及油脂等成分，积累的凝固油层/块会在膜表面形成可压缩的污染油层，导致膜通量的迅速衰减，而这不仅会增大设备的负荷，甚至会导致过程的不可行。The use of rectification separation process will lead to a sharp increase in transformation costs and operating costs, while the use of extraction process will also lead to the introduction of new pollutants. Adsorbents such as activated carbon and molecular sieve have a good adsorption effect on stearic acid and oil, but cannot remove highly water-soluble pollutants such as glycerin. Due to the limitation of filtration accuracy, dissolved organic matter cannot be removed by conventional plate and frame filtration, and the membrane separation equipment that can intercept molecules is directly used. Since the wastewater contains stearic acid and oil and other components, the accumulated solidified oil layer/block A compressible contaminated oil layer will be formed on the surface of the membrane, resulting in a rapid attenuation of the membrane flux, which will not only increase the load on the equipment, but even lead to the infeasibility of the process.
在现有生产情况下，实现硬脂酸甘油浓缩下水的合理有效治理，成为企业亟待结决的一个问题。Under the current production conditions, realizing the reasonable and effective management of stearic acid glycerin concentrated sewage has become a problem to be solved urgently by enterprises.
发明内容Contents of the invention
本发明要解决的技术问题是：基于上述问题，本发明提供一种硬脂酸生产中甘油浓缩下水的处理方法。The technical problem to be solved in the present invention is: based on the above problems, the present invention provides a treatment method for concentrated glycerin offal in stearic acid production.
本发明解决其技术问题所采用的一个技术方案是：一种硬脂酸生产中甘油浓缩下水的处理方法，针对工业硬脂酸生产中甘油浓缩下水，原水收集池中的甘油浓缩下水依次流经MBR过滤系统、一级RO处理系统和二级RO处理系统，MBR过滤系统的浓水输出端连接有生化处理系统的输入端，MBR过滤系统的淡水输出端与一级RO处理系统的输入端连接，一级RO处理系统的浓水输出端与二级RO处理系统的输入端连接，二级RO处理系统的淡水输出端与一级RO处理系统的输入端连接。A technical scheme adopted by the present invention to solve the technical problem is: a treatment method for concentrated glycerin offal in stearic acid production, aiming at the concentrated glycerin offwater in industrial stearic acid production, the concentrated glycerin offwater in the raw water collection pool flows through the MBR filtration system, primary RO treatment system and secondary RO treatment system, the concentrated water output of the MBR filtration system is connected to the input of the biochemical treatment system, and the fresh water output of the MBR filtration system is connected to the input of the primary RO treatment system , the concentrated water output end of the primary RO treatment system is connected to the input end of the secondary RO treatment system, and the fresh water output end of the secondary RO treatment system is connected to the input end of the primary RO treatment system.
进一步地，原水收集池的输出端与MBR过滤系统的输入端之间设有砂过滤器。Further, a sand filter is provided between the output end of the raw water collection tank and the input end of the MBR filtration system.
进一步地，MBR过滤系统的输出端与一级RO处理系统的输入端之间依次连接有中间水箱和碳滤精滤器，MBR过滤系统的淡水输出端与中间水箱的输入端连接，碳滤精滤器的输出端与一级RO处理系统的输入端连接，二级RO处理系统的淡水输出端与中间水箱的输入端连接。Further, an intermediate water tank and a carbon fine filter are sequentially connected between the output end of the MBR filter system and the input end of the primary RO treatment system, the fresh water output end of the MBR filter system is connected to the input end of the intermediate water tank, and the carbon filter fine filter The output end of the tank is connected to the input end of the primary RO treatment system, and the fresh water output end of the secondary RO treatment system is connected to the input end of the intermediate water tank.
进一步地，生化处理系统的输出端与原水收集池的输入端连接。Further, the output end of the biochemical treatment system is connected to the input end of the raw water collection tank.
进一步地，一级RO处理系统的淡水输出端与原水收集池的输入端之间依次连接有回用水箱和循环冷却水系统，一级RO处理系统的淡水输出端与回用水箱的输入端连接，循环冷却水系统的输出端与原水收集池的输入端连接。Further, the fresh water output end of the primary RO treatment system and the input end of the raw water collection tank are sequentially connected with a reuse water tank and a circulating cooling water system, and the fresh water output end of the primary RO treatment system is connected with the input end of the reuse water tank , the output end of the circulating cooling water system is connected with the input end of the raw water collection tank.
进一步地，二级RO处理系统的浓水输出端中的有机组分回收甘油或焚烧处理。Further, the organic components in the concentrated water output end of the secondary RO treatment system recover glycerin or incinerate.
进一步地，生化处理系统包括厌氧处理及耗氧处理，一级RO处理系统和二级RO处理系统均为反渗透膜过滤系统。Further, the biochemical treatment system includes anaerobic treatment and aerobic treatment, and the primary RO treatment system and the secondary RO treatment system are both reverse osmosis membrane filtration systems.
本发明的有益效果是：(1)产水水质好：COD值低、电导率低、无色澄清，相关指标满足GB8978-1996国标要求，可考虑回用，可回用至硬脂酸生产岗位或做循环冷却水；(2)生产过程稳定：过程可控、设备运转稳定；(3)处理成本低：与现有生化系统相比，处理同体积污水，在提高处理效果的同时，可减少人力、能耗、场地等相关费用，经一次处理粗估吨污水处理费用不高于5元；(4)绿色环保：可回收浓水中有机物和产水，并避免后继沼气、恶臭气体的处理等繁琐问题，浓水可去水解工序、返回甘油蒸发浓缩系统。The beneficial effects of the present invention are: (1) The quality of the produced water is good: the COD value is low, the electrical conductivity is low, colorless and clear, and the relevant indicators meet the requirements of the GB8978-1996 national standard, and can be considered for reuse, and can be reused in stearic acid production posts Or make circulating cooling water; (2) Stable production process: the process is controllable and the equipment runs stably; (3) Low treatment cost: Compared with the existing biochemical system, the same volume of sewage can be treated while improving the treatment effect, and can reduce Manpower, energy consumption, site and other related costs, after one treatment, the estimated cost per ton of sewage treatment is no more than 5 yuan; (4) Green environmental protection: organic matter and produced water in concentrated water can be recycled, and subsequent cumbersome treatment of biogas and malodorous gas can be avoided Problem, the concentrated water can go to the hydrolysis process and return to the glycerin evaporation and concentration system.
附图说明Description of drawings
下面结合附图对本发明进一步说明。The present invention will be further described below in conjunction with the accompanying drawings.
图1是本发明的结构示意图；Fig. 1 is a structural representation of the present invention;
其中：1.原水收集池，2.MBR过滤系统，3.一级RO处理系统，4.二级RO处理系统，5.生化处理系统，6.砂过滤器，7.中间水箱，8.碳滤精滤器，9.回用水箱，10.循环冷却水系统。Among them: 1. Raw water collection tank, 2. MBR filtration system, 3. Primary RO treatment system, 4. Secondary RO treatment system, 5. Biochemical treatment system, 6. Sand filter, 7. Intermediate water tank, 8. Carbon Fine filter, 9. Recycling water tank, 10. Circulating cooling water system.
具体实施方式detailed description
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。The present invention will now be further described in conjunction with specific examples, and the following examples are intended to illustrate the present invention rather than further limit the present invention.
一种硬脂酸生产中甘油浓缩下水的处理方法，针对工业硬脂酸生产中甘油浓缩下水，原水收集池1中的甘油浓缩下水依次流经MBR过滤系统2、一级RO处理系统3和二级RO处理系统4，MBR过滤系统2的浓水输出端连接有生化处理系统5的输入端，MBR过滤系统2的淡水输出端与一级RO处理系统3的输入端连接，一级RO处理系统3的浓水输出端与二级RO处理系统4的输入端连接，二级RO处理系统4的淡水输出端与一级RO处理系统3的输入端连接。A treatment method for concentrated glycerin off-water in stearic acid production, aiming at the concentrated off-water of glycerin in industrial stearic acid production, the concentrated off-water of glycerin in the raw water collection pool 1 flows through the MBR filtration system 2, the primary RO treatment system 3 and the second The first-stage RO treatment system 4, the concentrated water output of the MBR filtration system 2 is connected to the input of the biochemical treatment system 5, the fresh water output of the MBR filtration system 2 is connected to the input of the first-stage RO treatment system 3, and the first-stage RO treatment system The concentrated water output end of 3 is connected to the input end of the secondary RO treatment system 4 , and the fresh water output end of the secondary RO treatment system 4 is connected to the input end of the primary RO treatment system 3 .
原水收集池1的输出端与MBR过滤系统2的输入端之间设有砂过滤器6。A sand filter 6 is provided between the output end of the raw water collection tank 1 and the input end of the MBR filtration system 2 .
MBR过滤系统2的输出端与一级RO处理系统3的输入端之间依次连接有中间水箱7和碳滤精滤器8，MBR过滤系统2的淡水输出端与中间水箱7的输入端连接，碳滤精滤器8的输出端与一级RO处理系统3的输入端连接，二级RO处理系统4的淡水输出端与中间水箱7的输入端连接。An intermediate water tank 7 and a carbon fine filter 8 are sequentially connected between the output end of the MBR filtration system 2 and the input end of the primary RO treatment system 3, the fresh water output end of the MBR filtration system 2 is connected to the input end of the intermediate water tank 7, and the carbon The output end of the fine filter 8 is connected to the input end of the primary RO treatment system 3 , and the fresh water output end of the secondary RO treatment system 4 is connected to the input end of the intermediate water tank 7 .
生化处理系统5的输出端与原水收集池1的输入端连接。The output end of the biochemical treatment system 5 is connected with the input end of the raw water collection tank 1 .
一级RO处理系统3的淡水输出端与原水收集池1的输入端之间依次连接有回用水箱9和循环冷却水系统10，一级RO处理系统3的淡水输出端与回用水箱9的输入端连接，循环冷却水系统10的输出端与原水收集池1的输入端连接。The fresh water output end of the first-level RO treatment system 3 and the input end of the raw water collection tank 1 are connected in turn with a reuse water tank 9 and a circulating cooling water system 10, and the fresh water output end of the first-level RO treatment system 3 is connected with the return water tank 9. The input end is connected, and the output end of the circulating cooling water system 10 is connected with the input end of the raw water collection tank 1 .
二级RO处理系统4的浓水输出端中的有机组分回收甘油或焚烧处理。The organic component in the concentrated water output end of the secondary RO treatment system 4 recovers glycerin or incinerates it.
生化处理系统5包括厌氧处理及耗氧处理，一级RO处理系统3和二级RO处理系统4均为反渗透膜过滤。The biochemical treatment system 5 includes anaerobic treatment and aerobic treatment, and the primary RO treatment system 3 and the secondary RO treatment system 4 are reverse osmosis membrane filtration.
利用上述硬脂酸生产中甘油浓缩下水的处理方法的具体步骤为：Utilize the concrete steps of the treatment method of glycerol concentrated offwater in the above-mentioned stearic acid production to be:
步骤1、硬脂酸生产中甘油浓缩下水进入原水收集池中，送入砂过滤器中以降低废水浊度后，再送入MBR过滤系统中进行过滤分离，输出端的浓水和淡水的比例为1：4。Step 1. Glycerin concentration in the production of stearic acid enters the raw water collection tank, sends it to the sand filter to reduce the turbidity of the wastewater, and then sends it to the MBR filtration system for filtration and separation. The ratio of concentrated water to fresh water at the output end is 1 :4.
步骤2、经过MBR过滤系统分离后的浓水进入生化处理系统，硬脂酸、油脂等非均相有机物及粉尘等污染物在MBR过滤系统及与生化处理形成的半循环系统内循环，可被生化系统降解；淡水流向中间水箱进行储存后送入碳滤精滤器中后通入两级膜过滤系统。Step 2. The concentrated water separated by the MBR filter system enters the biochemical treatment system, and pollutants such as stearic acid, grease and other heterogeneous organic matter and dust circulate in the MBR filter system and the semi-circulation system formed with the biochemical treatment, which can be processed The biochemical system is degraded; the fresh water flows to the intermediate water tank for storage, then is sent to the carbon filter fine filter, and then passes through the two-stage membrane filtration system.
步骤3、在一级RO处理系统中，输出端的浓水和淡水比例为1：3，浓水进入二级RO处理系统；二级RO处理系统中，输出端的浓水和淡水比例为1：1，浓水中的有机组分回收甘油或焚烧处理，淡水流向中间水箱继续循环。RO处理系统均需加入阻垢剂，并定期加入清洗剂。Step 3. In the primary RO treatment system, the ratio of concentrated water to fresh water at the output end is 1:3, and the concentrated water enters the secondary RO treatment system; in the secondary RO treatment system, the ratio of concentrated water to fresh water at the output end is 1:1 , the organic components in the concentrated water are recycled to glycerin or incinerated, and the fresh water flows to the intermediate water tank to continue to circulate. All RO treatment systems need to add scale inhibitors, and regularly add cleaning agents.
步骤4、一级RO处理系统中分离出的淡水进入回用水箱，可用作循环冷却系统供水，其中被蒸发出水可以用于生产环节或循环水，剩下部分水送入原水收集池中起稀释浓缩下水作用。Step 4. The fresh water separated from the first-level RO treatment system enters the reuse water tank and can be used as water supply for the circulating cooling system. The evaporated water can be used for production links or circulating water, and the remaining part of the water is sent to the raw water collection tank for recovery. Dilute and concentrate sewer effect.
甘油浓缩下水中的主要有机成分为甘油、硬脂酸和微量油脂，随着RO膜浓缩处理过程的进行，保留液侧的有机物浓度逐渐增长。虽然硬脂酸及油脂难溶于水，但由于可与水互溶的甘油的存在，在本发明处理工艺中，硬脂酸和油脂能够溶于甘油水中，这避免了硬脂酸/油脂在RO处理系统的处理过程中作为非均相物质析出，从而缓解了膜表面的污染，使得处理过程能顺利进行。The main organic components in the glycerin concentrated water are glycerin, stearic acid and a small amount of oil. With the RO membrane concentration process, the concentration of organic matter on the retentate side gradually increases. Although stearic acid and oil are insoluble in water, due to the existence of water-miscible glycerin, in the treatment process of the present invention, stearic acid and oil can be dissolved in glycerin water, which avoids stearic acid/oil in the RO During the treatment process of the treatment system, it is precipitated as a heterogeneous substance, thereby alleviating the pollution of the membrane surface and making the treatment process go smoothly.
与原处理工艺相比，本发明方法具有产水质量好、生化处理污水体积总量少的明显优势，实现了甘油浓缩下水的资源化处理。在目前水处理现状下，如需展开本发明工作，可深入进行相关实验工作。Compared with the original treatment process, the method of the present invention has the obvious advantages of good water quality and less total volume of biochemically treated sewage, and realizes the resourceful treatment of concentrated glycerin sewage. Under the current status of water treatment, if the work of the present invention needs to be carried out, relevant experimental work can be carried out in depth.
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。Inspired by the above-mentioned ideal embodiment according to the present invention, through the above-mentioned description content, relevant workers can make various changes and modifications within the scope of not departing from the technical idea of the present invention. The technical scope of the present invention is not limited to the content in the specification, but must be determined according to the scope of the claims.
Claims (7)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610878610.0A CN106348530A (en) | 2016-09-30 | 2016-09-30 | Treatment method for glycerine concentrated sewage of stearic acid production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610878610.0A CN106348530A (en) | 2016-09-30 | 2016-09-30 | Treatment method for glycerine concentrated sewage of stearic acid production |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106348530A true CN106348530A (en) | 2017-01-25 |
Family
ID=57866391
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610878610.0A Pending CN106348530A (en) | 2016-09-30 | 2016-09-30 | Treatment method for glycerine concentrated sewage of stearic acid production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106348530A (en) |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101402509A (en) * | 2008-11-21 | 2009-04-08 | 北京桑德环境工程有限公司 | Treatment system and method for high-salt wastewater |
| CN201309875Y (en) * | 2008-12-08 | 2009-09-16 | 核工业理化工程研究院华核新技术开发公司 | Recycling device of biological pharmaceutical wastewater |
| CN101792216A (en) * | 2010-02-09 | 2010-08-04 | 丁国良 | Resource recycling method of glyphosate mother liquor |
| CN202152307U (en) * | 2011-05-12 | 2012-02-29 | 北京美能环保科技有限公司 | A Submerged Membrane Bioreactor |
| CN104230083A (en) * | 2014-08-21 | 2014-12-24 | 波鹰(厦门)科技有限公司 | Method for recovering sodium chloride and glycerol from high-salt glycerol-containing high-depth organic wastewater |
| CN105417835A (en) * | 2014-09-12 | 2016-03-23 | 深圳市嘉泉膜滤设备有限公司 | Sewage treatment and seawater desalination process method |
| CN105859019A (en) * | 2016-03-22 | 2016-08-17 | 中国环境科学研究院 | Treating and recycling method and apparatus for organic wastewater |
-
2016
- 2016-09-30 CN CN201610878610.0A patent/CN106348530A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101402509A (en) * | 2008-11-21 | 2009-04-08 | 北京桑德环境工程有限公司 | Treatment system and method for high-salt wastewater |
| CN201309875Y (en) * | 2008-12-08 | 2009-09-16 | 核工业理化工程研究院华核新技术开发公司 | Recycling device of biological pharmaceutical wastewater |
| CN101792216A (en) * | 2010-02-09 | 2010-08-04 | 丁国良 | Resource recycling method of glyphosate mother liquor |
| CN202152307U (en) * | 2011-05-12 | 2012-02-29 | 北京美能环保科技有限公司 | A Submerged Membrane Bioreactor |
| CN104230083A (en) * | 2014-08-21 | 2014-12-24 | 波鹰(厦门)科技有限公司 | Method for recovering sodium chloride and glycerol from high-salt glycerol-containing high-depth organic wastewater |
| CN105417835A (en) * | 2014-09-12 | 2016-03-23 | 深圳市嘉泉膜滤设备有限公司 | Sewage treatment and seawater desalination process method |
| CN105859019A (en) * | 2016-03-22 | 2016-08-17 | 中国环境科学研究院 | Treating and recycling method and apparatus for organic wastewater |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100545112C (en) | Reuse treatment method of chemical plasticizer wastewater | |
| CN102001794B (en) | Method for treating unsaturated polyester resin production wastewater | |
| CN205170626U (en) | Organic high salt concentration effluent disposal system | |
| CN1278962C (en) | Reuse method of leachate from municipal solid waste landfill | |
| CN203530059U (en) | Treatment system of waste drilling mud filtrate | |
| CN103613071A (en) | Method for recycling bromine from bromine-containing wastewater of brominated butyl rubber | |
| CN102452759A (en) | Technology for treating gasoline alkali residues | |
| CN105439386B (en) | Deep treatment method and device for hazardous waste physical and chemical treatment unit | |
| CN104230124B (en) | Coal chemical industry wastewater zero emission technique and specific equipment thereof | |
| CN104291522A (en) | Method for treating industrial wastewater | |
| CN103626353A (en) | Method for processing city household garbage leachate | |
| CN100509662C (en) | Oil refinery sewage treatment and reusing process system and operation method thereof | |
| CN106315973A (en) | Treatment method of high-salt and high-calcium industrial wastewater | |
| CN204325082U (en) | A kind for the treatment of system of papermaking midcourse wastewater | |
| CN101921046B (en) | Process for treating coal gasification wastewater by using active coke | |
| CN104386881A (en) | Coal chemical production wastewater treatment and high-efficiency recycling process and special system thereof | |
| CN102092903B (en) | Process for treating and recycling di-tertiary-butyl peroxide production waste water | |
| CN1594143A (en) | Treatment method for gas wash water | |
| CN103288306A (en) | Process for treating heavy oil waste water | |
| CN105800864A (en) | Zero discharge method for waste liquid of water-based ink | |
| CN101838084B (en) | Biochemical regulation and treatment process for sewage of urban domestic garbage transfer station | |
| CN103864239A (en) | Circulating purifying water | |
| CN107792963A (en) | Landfill Leachate handling process and its special equipment | |
| CN106348530A (en) | Treatment method for glycerine concentrated sewage of stearic acid production | |
| CN204550278U (en) | A kind of electroplating waste-water reutilizing equipment |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20170125 |