CN101139117A - Technique for processing wastewater containing methanol and dimethyl ether - Google Patents
Technique for processing wastewater containing methanol and dimethyl ether Download PDFInfo
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- CN101139117A CN101139117A CNA2007100549875A CN200710054987A CN101139117A CN 101139117 A CN101139117 A CN 101139117A CN A2007100549875 A CNA2007100549875 A CN A2007100549875A CN 200710054987 A CN200710054987 A CN 200710054987A CN 101139117 A CN101139117 A CN 101139117A
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Abstract
The present invention discloses a wastewater treatment technics containing methanol and dimethyl ether and solves the problem that the wastewater produced by MTO device can not meet the need of the water inlet quality of wastewater treatment plant. The technics of the present invention includes that the wastewater containing methanol and dimethyl ether enters a dimethyl ether stripping tower after heat exchange. The top of the tower generates gas mixtures of dimethyl ether, etc. The bottom of the tower generates water containing methanol. The water containing methanol enters into a methanol stripping tower after heat exchange and pressuring. The top of the methanol stripping tower generates methanol gas which enters a methanol reflux drum after being cooled. After lifting pressure, part of the methanol gas return to the top of the methanol stripping tower as reflux and the other part as the products of methanol. The bottom of the methanol stripping tower generates purified water. The total content of methanol and dimethyl ether in the purified water acquired after treated by the technics of the present invention is less than or equal to 100ppm and the purified water can meet the need of the water inlet quality of wastewater treatment plant.
Description
Technical field
The invention belongs to sewage treatment area.Be particularly related to a kind of sewage treatment process that contains methyl alcohol and dme.
Background technology
Commercial run such as refining of petroleum, petrochemical complex tends to produce sewage, as not handling contaminate environment seriously in good time, and makes the resource loss that can effectively utilize.Produce alkene technology (MTO) by coal or natural gas via methyl alcohol and be in the technological development forward position in the world, have significantly competition potential.Under the higher situation of present oil price, be about to step into the industrial applications stage by coal or natural gas via preparing light olefins from methanol in the world.Owing to contain objectionable impuritiess such as small amount of methanol toxic substance and dme in the sewage that preparing low carbon olefinic hydrocarbon with methanol device (hereinafter to be referred as the MTO device) produces, if this sewage is not carried out pre-treatment, handle and directly be discharged to the sewage-farm, then can not satisfy sewage-farm feedwater quality requirement, can not guarantee that the normal operation in sewage-farm and final sewage of discharging outside the factory meet the requirements of the standard.All can be used as the raw material of MTO device again because of methyl alcohol and dme,, can reclaim, then can turn harm into good, save the raw material of producing low-carbon alkene these two kinds of materials in the sewage if when disposing of sewage.Especially what deserves to be mentioned is that dme is except that producing the low-carbon alkene, it still is good methylating reagent, can be used for producing dimethyl sulfate, dimethyl carbonate, dimethyl thioether and methine halide etc.Dme can be used as plastics blowing agent, can make the hole of porous plastics even, and snappiness and resistance to pressure improve, and application prospect is good.Dme also can be used as refrigeration agent.Dme is guaranteed it because of the combustionproperty of excellence and be can be used as the surrogate of green diesel motor spirit, liquefied petroleum gas (LPG), alcohol-ether fuel main component and automobile-used oil additive etc.Because therefore above-mentioned numerous purposes of dme if when disposing of sewage, can reclaim dme material in the sewage, obtain purer dme, except that the raw material of producing low-carbon alkene, also can make other purposes, then this sewage water treatment method is reasonable.
CN1508083A discloses a kind of technology and device that contains the methanol condensed water handling reclamation, its concrete grammar is: turn to main method with biological contact oxidation and handle containing methanol condensed water, under aerobic condition with waste water in a small amount of organic matter degradation such as methyl alcohol, processed water of condensation uses through can be used as water of productive use after the solid-liquid separation.The water that bio-contact oxidation is handled also can utilize ozone to carry out further oxidation, makes dissolved organic matter residual in the water and microorganism secretion thing obtain decomposing, and formation can be by the organic acid of follow-up ion remaval system removal.After a series of processing such as bio-contact oxidation, ozone oxidation and ion remaval, water of condensation can be used as deionized water and obtains reuse.But this technology can not be handled the sewage that contains materials such as methyl alcohol and dme simultaneously, also the document announcement of not finding relevant this kind waste disposal plant at present.
Summary of the invention
The sewage that The present invention be directed to the generation of MTO device does not satisfy the requirement of sewage-farm feedwater quality, and a kind of technology that the sewage that contains methyl alcohol and dme is handled is provided.Use that methyl alcohol and two kinds of material gross weights of dme content are not more than 100ppm in the purifying waste water of obtaining after the art breading of the present invention, satisfy sewage-farm feedwater quality requirement, and can reclaim environmentally harmful materials such as methyl alcohol in the sewage and dme, the raw material that they both can be used as preparing low carbon olefinic hydrocarbon with methanol returns the MTO device, also can be used as other purposes.
Technical scheme of the present invention is: the sewage that contains methyl alcohol and dme, enter the dme stripping tower, dme stripping tower cat head produces gaseous mixture such as dme, go out to contain methanol-water at the bottom of the dme stripping Tata, contain methanol-water through heat exchange, enter methanol stripper tower after the pressurization, the methanol stripper tower cat head produces methanol gas, after cooling, a part is returned the methanol stripper tower cat head as backflow, another part goes out to purify waste water at the bottom of the methanol stripper tower tower as methanol product, delivers to outside the device, the methanol stripper tower reflux ratio is 1～80, the gaseous mixture such as dme that wherein said dme stripping tower cat head produces enter return tank after the cooling, the liquid phase of return tank is returned dme stripping tower cat head as backflow, the gaseous stream of return tank, after being condensed into liquid phase as product dimethyl ether; Perhaps enter return tank after cooling condensation becomes liquid phase, a part is returned dme stripping tower cat head as backflow, and another part is as product dimethyl ether.
Dme stripping tower of the present invention is divided into two sections, and cat head is a rectifying section to feed entrance, and feed entrance is a stripping section at the bottom of tower, and the dme stripping tower has 20～55 theoretical stages, and its opening for feed is opened from 8th～30 piece theoretical stage of cat head to the tower truth of a matter; Dme stripping tower cat head working pressure is 0.1～1.2MPa, is preferably 0.3～0.6Mpa; Dme stripping tower column bottom temperature is 100～190 ℃, is preferably 130～165 ℃; Be that the steam of 0.2～2.0MPa heats stripping by reboiler with pressure at the bottom of the dme stripping Tata, the most handy pressure is the steam of 0.5～1.0MPa.
The service temperature of dme stripping tower return tank of the present invention is-25～55 ℃, is preferably 5～45 ℃.
Methanol stripper tower of the present invention is divided into two sections, cat head is a rectifying section to feed entrance, and feed entrance is a stripping section at the bottom of tower, and methanol stripper tower has 40～70 theoretical stages, its opening for feed is opened from 10th～35 piece theoretical stage of cat head to the tower truth of a matter, preferentially at 13-20 piece theoretical stage place.Methanol stripper tower cat head working pressure is 0.05～1.2MPa, is preferably 0.1～0.3Mpa; The methanol stripper tower column bottom temperature is 90 ℃～190 ℃, is preferably 110～140 ℃.
Be that the steam of 0.2～2.0MPa heats stripping by reboiler with pressure at the bottom of the methanol stripper tower tower of the present invention, the most handy pressure is the steam of 0.3～0.7MPa.
Methanol stripper tower return tank service temperature of the present invention is 20～100 ℃, is preferably 35～60 ℃.
The sewage treatment process that contains methyl alcohol and dme of the present invention is specially adapted to handle the sewage that converting methanol to prepare low carbon olefin (MTO) device produces.
The invention has the beneficial effects as follows:
1) technology of the present invention can be handled the sewage that the MTO device produces, obtain after treatment purify waste water in methyl alcohol and two kinds of material gross weights of dme content be not more than 100ppm, satisfy sewage-farm feedwater quality requirement.
2) technology of the present invention can reclaim environmentally harmful materials such as methyl alcohol in the sewage and dme, the methanol product that recovery obtains and the purity of product dimethyl ether can both reach more than the 90 weight %, higher reaches more than the 95 weight %, can reach more than the 99 weight %.The raw material that they both can be used as preparing low carbon olefinic hydrocarbon with methanol returns the MTO device, also can be used as other purposes.
3) technology of the present invention is carried out stripping because of adopting double tower, flexible operation, subject range to methyl alcohol in the sewage and dme concentration is wide, though total steam consumption is bigger, but because the methanol stripper tower working pressure is low, therefore can adopt factory in the little low-pressure steam of purposes to carry out stripping, saving general facilities expense.
Describe the present invention in detail below by the drawings and specific embodiments, but do not limit the scope of the invention.
Description of drawings
Fig. 1 is a kind of simple flow chart of technology of the present invention.
Fig. 2 is the another kind of simple flow chart of technology of the present invention.
Reference numeral shown in the figure is:
The 1-sump pump, 2-interchanger, 3-dme stripping tower, 4-reboiler, 5-water cooler, the 6-return tank, the 7-reflux pump, 8-condenser, 9-contain pure water pump, the 10-methanol stripper tower, 11-methanol gas condensate cooler, 12-methanol eddy jar, 13-methanol eddy pump, 14-methanol stripper tower reboiler.
Embodiment
As shown in Figure 1, the sewage that contains methyl alcohol and dme, by sump pump 1 pressurization, again through interchanger 2 with come out at the bottom of dme stripping tower 3 towers contain the methanol-water heat exchange after enter dme stripping tower 3, dme stripping tower 3 cats head produce gaseous mixture such as dme, after water cooler 5 coolings, enter return tank 6, liquid phase stream in the return tank 6, after reflux pump 7 boosts, return dme stripping tower 3 cats head as backflow, the dme vapor phase stream in the return tank 6 is condensed into liquid phase as product dimethyl ether through condenser 8, the raw material that product dimethyl ether can be used as preparing low carbon olefinic hydrocarbon with methanol returns MTO device reaction part, but also carrying device is made other purposes outward.Go out to contain methanol-water at the bottom of dme stripping tower 3 towers, heat strippings with steam by reboiler 4 at the bottom of dme stripping tower 3 towers, go out at the bottom of dme stripping tower 3 towers contain methanol-water with contain the sewage heat exchange of methyl alcohol and dme after, after containing pure water pump 9 pressurizations, enter methanol stripper tower 10, heat strippings with steam by methanol stripper tower reboiler 14 at the bottom of the tower of methanol stripper tower 10.The cat head of methanol stripper tower 10 produces methanol gas, methanol gas enters methanol eddy jar 12 after 11 coolings of methanol gas condensate cooler, then after methanol eddy pump 13 boosts, a part is returned methanol stripper tower 10 cats head as backflow, another part is as methanol product, the raw material that this product can be used as preparing low carbon olefinic hydrocarbon with methanol returns MTO device reaction part, but also carrying device is made other purposes outward, and preferentially the raw material as preparing low carbon olefinic hydrocarbon with methanol returns MTO device reaction part; Go out methyl alcohol at the bottom of methanol stripper tower 10 towers and two kinds of material gross weights of dme content is not more than purifying waste water of 100ppm, deliver to outside the device after the cooling.
What Fig. 2 was different with Fig. 1 is: the gaseous mixture such as dme that dme stripping tower 3 cats head produce, after being condensed into liquid phase, water cooler 5 and condenser 8 enter return tank 6, after reflux pump 7 boosted, a part was returned cat head as backflow, and another part is as product dimethyl ether.
Claims (10)
1. a sewage treatment process that contains methyl alcohol and dme is characterized in that comprising the steps:
The sewage that contains methyl alcohol and dme, enter the dme stripping tower after the heat exchange, dme stripping tower cat head produces gaseous mixture such as dme, go out to contain methanol-water at the bottom of the dme stripping Tata, contain methanol-water through heat exchange, enter methanol stripper tower after the pressurization, the methanol stripper tower cat head produces methanol gas, after cooling, a part is returned the methanol stripper tower cat head as backflow, another part goes out to purify waste water at the bottom of the methanol stripper tower tower as methanol product, delivers to outside the device, the methanol stripper tower reflux ratio is 1～80, the gaseous mixture such as dme that wherein said dme stripping tower cat head produces enter return tank after the cooling, the liquid phase of return tank is returned dme stripping tower cat head as backflow, the gaseous stream of return tank, after being condensed into liquid phase as product dimethyl ether; Perhaps enter return tank after cooling condensation becomes liquid phase, a part is returned dme stripping tower cat head as backflow, and another part is as product dimethyl ether;
Described dme stripping tower is divided into two sections, and cat head is a rectifying section to feed entrance, and feed entrance is a stripping section at the bottom of tower, and the dme stripping tower has 20～55 theoretical stages, and its opening for feed is opened from the 8-30 piece theoretical stage of cat head to the tower truth of a matter; Dme stripping tower cat head working pressure is 0.1～1.2MPa, and dme stripping tower column bottom temperature is 100～190 ℃, is that the steam of 0.2～2.0MPa heats stripping by reboiler with pressure at the bottom of the dme stripping Tata;
Described methanol stripper tower is divided into two sections, cat head is a rectifying section to feed entrance, feed entrance is a stripping section at the bottom of tower, methanol stripper tower has 40～70 theoretical stages, its opening for feed is opened from the 10-35 piece theoretical stage of cat head to the tower truth of a matter, methanol stripper tower cat head working pressure is 0.05～1.2MPa, and the methanol stripper tower column bottom temperature is 90 ℃～190 ℃, is that the steam of 0.2～2.0MPa heats stripping by reboiler with pressure at the bottom of the methanol stripper tower tower.
2. technology according to claim 1 is characterized in that: described dme stripping tower cat head working pressure is 0.3～0.6Mpa; Dme stripping tower column bottom temperature is 130～165 ℃.
3. technology according to claim 1 is characterized in that: described methanol stripper tower cat head working pressure is 0.1～0.3Mpa; The methanol stripper tower column bottom temperature is 110～140 ℃.
4. technology according to claim 1 is characterized in that: be that the steam of 0.5～1.0MPa heats stripping by reboiler with pressure at the bottom of the described dme stripping Tata.
5. technology according to claim 1 is characterized in that: the service temperature of described dme stripping tower return tank is-25～55 ℃.
6. technology according to claim 5 is characterized in that: the service temperature of described dme stripping tower return tank is 5～45 ℃.
7. technology according to claim 1 is characterized in that: be that the steam of 0.3～0.7MPa heats stripping by reboiler with pressure at the bottom of the described methanol stripper tower tower.
8. technology according to claim 1 is characterized in that: described methanol stripper tower return tank service temperature is 20～100 ℃.
9. technology according to claim 8 is characterized in that: described methanol stripper tower return tank service temperature is 35～60 ℃.
10. technology according to claim 1 is characterized in that: described methanol stripper tower opening for feed is opened from the 13-20 piece theoretical stage of cat head to the tower truth of a matter.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CNB2007100549875A CN100548895C (en) | 2007-08-17 | 2007-08-17 | The sewage treatment process that contains methyl alcohol and dme |
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| CNB2007100549875A CN100548895C (en) | 2007-08-17 | 2007-08-17 | The sewage treatment process that contains methyl alcohol and dme |
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| CN101139117A true CN101139117A (en) | 2008-03-12 |
| CN100548895C CN100548895C (en) | 2009-10-14 |
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Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102442744A (en) * | 2010-09-30 | 2012-05-09 | 中国石油化工股份有限公司 | Treatment method of high-concentration process waste water during methanol-to-olefin process |
| CN102060404B (en) * | 2009-11-17 | 2012-11-21 | 中国石油化工集团公司 | Sewage treatment method for recycling low-carbon hydrocarbons and low-carbon oxygen-containing organic matters |
| CN102951983A (en) * | 2011-08-25 | 2013-03-06 | 中国石油化工股份有限公司 | Method for reducing energy consumption of device for preparing olefins from oxy-compound |
| CN103030184A (en) * | 2012-11-27 | 2013-04-10 | 常州大学 | Water treatment solvent recovery method |
| CN104271512A (en) * | 2012-04-26 | 2015-01-07 | 博瑞立斯有限公司 | Method for reducing organic impurities in waste water |
| CN104556541A (en) * | 2013-10-22 | 2015-04-29 | 中国石油化工股份有限公司 | Treatment method of MTG (Methanol To Gasoline) technology generation water |
| CN106045822A (en) * | 2016-05-25 | 2016-10-26 | 长岭炼化岳阳工程设计有限公司 | Energy-saving phenol refining device with high product segmentation degree, and phenol refining method |
| CN106039750A (en) * | 2016-05-30 | 2016-10-26 | 长岭炼化岳阳工程设计有限公司 | Vacuum four-column differential pressure thermal coupling device and method for refining of crude phenol |
| CN107362563A (en) * | 2017-08-22 | 2017-11-21 | 南通泰利达化工有限公司 | The ethanol distillation technique and device of a kind of nitrocotton |
| CN108191594A (en) * | 2017-11-10 | 2018-06-22 | 中国天辰工程有限公司 | A kind of preprocess method of MTO devices spent lye |
| CN109534302A (en) * | 2018-11-13 | 2019-03-29 | 乳源东阳光电化厂 | A kind of method and its application for removing dimethyl sulfate in sulfuric acid |
| CN111285421A (en) * | 2020-01-16 | 2020-06-16 | 董国亮 | Methanol-to-olefin sewage stripping tower system |
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2007
- 2007-08-17 CN CNB2007100549875A patent/CN100548895C/en active Active
Cited By (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102060404B (en) * | 2009-11-17 | 2012-11-21 | 中国石油化工集团公司 | Sewage treatment method for recycling low-carbon hydrocarbons and low-carbon oxygen-containing organic matters |
| CN102442744A (en) * | 2010-09-30 | 2012-05-09 | 中国石油化工股份有限公司 | Treatment method of high-concentration process waste water during methanol-to-olefin process |
| CN102442744B (en) * | 2010-09-30 | 2013-07-03 | 中国石油化工股份有限公司 | Treatment method of high-concentration process waste water during methanol-to-olefin process |
| CN102951983B (en) * | 2011-08-25 | 2016-01-13 | 中国石油化工股份有限公司 | A kind of method reducing oxygenatedchemicals olefin hydrocarbon apparatus energy consumption |
| CN102951983A (en) * | 2011-08-25 | 2013-03-06 | 中国石油化工股份有限公司 | Method for reducing energy consumption of device for preparing olefins from oxy-compound |
| CN104271512B (en) * | 2012-04-26 | 2016-08-24 | 博瑞立斯有限公司 | For the method reducing the organic impurities in waste water |
| CN104271512A (en) * | 2012-04-26 | 2015-01-07 | 博瑞立斯有限公司 | Method for reducing organic impurities in waste water |
| CN103030184A (en) * | 2012-11-27 | 2013-04-10 | 常州大学 | Water treatment solvent recovery method |
| CN104556541A (en) * | 2013-10-22 | 2015-04-29 | 中国石油化工股份有限公司 | Treatment method of MTG (Methanol To Gasoline) technology generation water |
| CN104556541B (en) * | 2013-10-22 | 2017-03-01 | 中国石油化工股份有限公司 | A kind of processing method of preparing gasoline by methanol Process Production water |
| CN106045822A (en) * | 2016-05-25 | 2016-10-26 | 长岭炼化岳阳工程设计有限公司 | Energy-saving phenol refining device with high product segmentation degree, and phenol refining method |
| CN106039750A (en) * | 2016-05-30 | 2016-10-26 | 长岭炼化岳阳工程设计有限公司 | Vacuum four-column differential pressure thermal coupling device and method for refining of crude phenol |
| CN107362563A (en) * | 2017-08-22 | 2017-11-21 | 南通泰利达化工有限公司 | The ethanol distillation technique and device of a kind of nitrocotton |
| CN108191594A (en) * | 2017-11-10 | 2018-06-22 | 中国天辰工程有限公司 | A kind of preprocess method of MTO devices spent lye |
| CN109534302A (en) * | 2018-11-13 | 2019-03-29 | 乳源东阳光电化厂 | A kind of method and its application for removing dimethyl sulfate in sulfuric acid |
| CN111285421A (en) * | 2020-01-16 | 2020-06-16 | 董国亮 | Methanol-to-olefin sewage stripping tower system |
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| CN100548895C (en) | 2009-10-14 |
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