CN103553877B - Method for rectifying ethylene glycol during production of ethylene glycol from calcium carbide furnace gas - Google Patents
Method for rectifying ethylene glycol during production of ethylene glycol from calcium carbide furnace gas Download PDFInfo
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Abstract
The invention relates to a method for rectifying ethylene glycol during production of the ethylene glycol from calcium carbide furnace gas. A methanol recovery tower, a dehydration tower, a dealcoholization tower, an ethylene glycol refining tower and an ethylene glycol product recovery tower, which are sequentially connected are adopted. According to different impurities in a crude product in different periods, a key purification device of the ethylene glycol, namely a product tower adopts a sub-tower disk for feeding and a sub-tower disk side mining technology so as to improve the purity of an ethylene glycol product; in order to solve the problems of complex impurities in the crude ethylene glycol, easiness in formation of an azeotrope and influence on ultraviolet light transmittance, a method for reasonably replenishing the fine ethylene glycol is adopted for the main dealcoholization tower and the dehydration tower so as to purify the quality of the ethylene glycol. According to the method, the difficult problems of poor quality, small market share, incapability of implementing industrialization amplification and the like of the ethylene glycol product which is produced from coal in China are effectively solved, and the method has the advantages of high impurity removal rate, high product quality, economy, reasonableness, feasible process technology, safety and stability, and can achieve the purposes of reducing the impurities in the product and improving the product quality. The method provided by the invention can be applied to the method for rectifying the ethylene glycol during the production of the ethylene glycol from the calcium carbide furnace gas.
Description
Technical field
The present invention relates to ethylene glycol distillation technology, be specially adapted in the method for ethylene glycol rectifying in calcium carbide furnace gas preparing ethylene glycol.
Background technology
Ethylene glycol (EG) is one of important source material of Organic Chemical Industry, mainly for the production of vibrin and deicing fluid, also has a small amount of application in fields such as unsaturated polyester resin, lubricant, softening agent, nonionogenic tensides.
China is ethylene glycol country of consumption maximum in the world, and consumption accounts for 1/3 of the world.Within 2012, China's ethylene glycol demand reaches 1,050 ten thousand tons, and output reaches 3,500,000 tons, and importation dependence reaches more than 70%.Rapidly, the ethylene glycol of 90% is for the production of vibrin, and 10% for the production of deicing fluid, tackiness agent, paint solvent etc. for China's polyester industrial development, produces vibrin and requires that quality of ethylene glycol product reaches polyester grade requirement.
The production method of ethylene glycol mainly contains petroleum path and the large class of Non oil-based route two in the world at present, petroleum path technical maturity, and application is comparatively extensive, but the method affects fluctuation comparatively greatly by International Petroleum Price, and water is than large, and energy consumption is high, and production cost is higher.According to the resource situation of China's " oil-poor, rich coal, weak breath ", the coal-ethylene glycol technology of Non oil-based route is research and development direction from now on.
Since 2011, China's coal-ethylene glycol starts upsurge, but up to the present, coal-ethylene glycol technology is also immature, imperfect, one of Problems existing is quality product existing problems, quality of ethylene glycol product can only reach technical grade product, can not reach polyester grade requirement, polyester grade ethylene glycol requires more than 99.9% to product purity.Because hydrogenation reaction is a complicated chemosynthesis process, along with the work-ing life of catalyzer increases, side reaction also increases thereupon, and dopant species and content increase, make rectifying separation comparatively difficult, this is also the major cause that current domestic coal-ethylene glycol product can not reach polyester grade requirement.And ethylene glycol distillation system plays key effect to end product quality.Impurity in ethylene glycol crude product is methyl alcohol, ethanol, methyl glycolate, dimethyl oxalate, 1,2-butyleneglycol etc., the increase of above impurity brings the difficulty of purification to ethylene glycol distillation system, because ethylene glycol crude liquid boiling point is high, need vacuum operating and in feed liquid impurity is easily and ethylene glycol formation azeotrope, the elevation of boiling point, is more difficult to conventional rectification simultaneously.Therefore the ethylene glycol distillation technology of the feasible calcium carbide furnace gas preparing ethylene glycol of economical rationality, Technology is researched and developed, extremely urgent.
Coal Chemical Industry " 12 " planning proposes, and by 2015, basic grasp 200,000 ~ 300,000 tons of extensive complete set technologys of coal-ethylene glycol, possessed Project design construction and critical equipment manufacturing capacity.If the ethylene glycol product that synthetic gas method production polyester grade requires can not be realized, the rich coal of China will be caused not carry out deep processing, can not produce the polyester grade ethylene glycol product meeting downstream and require, have a strong impact on the energy general layout of China, can deepen further the interdependency of oil.
Summary of the invention
The invention reside in and solve that current China coal-ethylene glycol product foreign matter content is high, of poor quality, share of market is low, can not the difficult problem such as industrialization amplification, by designing and optimize the rectification section of ethylene glycol, so provide that a kind of removal of impurity is high, quality product is high, the method for ethylene glycol rectifying in calcium carbide furnace gas preparing ethylene glycol that economical rationality, Technology are feasible.
The technical solution used in the present invention is: the method for ethylene glycol rectifying in calcium carbide furnace gas preparing ethylene glycol of the present invention, comprises the methanol distillation column, dehydration tower, dealcoholize column, purifying ethylene glycol tower and the ethylene glycol product recovery tower that are connected successively, Methanol Recovery column overhead arranges one-level water cooler, secondary coolers, deep freezer, methanol distillation column return tank, vacuum system, dehydration column overhead arranges one-level water cooler, secondary coolers, deep freezer, dehydration tower return tank, vacuum system, dealcoholize column tower top arranges one-level water cooler, deep freezer, dealcoholize column return tank, vacuum system, purifying ethylene glycol column overhead arranges one-level water cooler, deep freezer, purifying ethylene glycol tower return tank, vacuum system, ethylene glycol product recovery tower tower top arranges one-level water cooler, deep freezer, ethylene glycol product recovery tower return tank, vacuum system.Adopt five tower rectification process flow processs, the main purpose of methanol distillation column reclaims the methyl alcohol in the thick alcohol product of hydrogenation, and reclaim product front-end volatiles (comprise dme, methyl-formiate etc.), the main purpose of dehydration tower is moisture in removing product and part lower boiling alcohols, ester class is (as C2-C5 alcohols, methyl glycolate, dimethyl oxalate), the main purpose of dealcoholize column removes glycols (as 2, 3-butyleneglycol, 1, 2-propylene glycol, 1, 2-butyleneglycol), purifying ethylene glycol tower main purpose obtains high-quality ethylene glycol product, the main purpose of glycol recovery tower proposes last running, reclaim the ethylene glycol of discharging at the bottom of purifying ethylene glycol tower tower.
The method of ethylene glycol rectifying in described calcium carbide furnace gas preparing ethylene glycol, comprises the steps:
1. the thick ethylene glycol from hydrogenation unit is after preheater and ethylene glycol product heat exchange, enter methanol distillation column bottom, methanol distillation column overhead gas is at one-level water cooler partial condensation, uncooled gas enters secondary condenser condensation, still uncooled gas enters deep freezer, non-condensable gas goes vacuum system, the phlegma of first-stage condenser and secondary condenser enters methanol distillation column return tank through being pumped into methanol distillation column trim the top of column, the phlegma of deep freezer enters front-end volatiles storage tank, methanol distillation column top survey line extraction refined methanol;
2. Methanol Recovery tower reactor liquid is in the middle part of pump delivery to dehydration tower, the condensation in first-stage condenser of dehydration column overhead gas, uncooled gas enters condensation in secondary condenser, still uncooled gas enters deep freezer, non-condensable gas goes vacuum system, the phlegma of first-stage condenser enters dehydration tower return tank through being pumped into dehydration column overhead backflow, and the phlegma of secondary condenser and deep freezer is potato spirit byproduct, enters potato spirit storage tank;
3. dehydrating tower kettle liquid is transported in the middle part of dealcoholize column, the condensation in first-stage condenser of dealcoholize column overhead gas, uncondensed gas sends into condensation in deep freezer, non-condensable gas goes vacuum system, the phlegma of first-stage condenser and deep freezer enters dealcoholize column return tank, phlegma delivers to dealcoholize column trim the top of column through reflux pump, and partial condensation liquid is delivered to lighting end surge tank and stored;
4. dealcoholysis tower bottoms through pump delivery to purifying ethylene glycol tower bottom, the condensation in first-stage condenser of purifying ethylene glycol column overhead gas, uncondensed gas sends into condensation in deep freezer, non-condensable gas goes vacuum system, the phlegma of first-stage condenser and deep freezer enters purifying ethylene glycol tower return tank, a phlegma part is through being pumped into the backflow of purifying ethylene glycol column overhead, and 98% 1 glycol storage tank is delivered in another part extraction;
5. purifying ethylene glycol tower top side take-off premium grads ethylene glycol product, ethylene glycol product after preheater and thick ethylene glycol heat exchange are lowered the temperature again through the laggard ethylene glycol product storage tank of condenser condenses;
6. purifying ethylene glycol tower bottoms is in the middle part of pump delivery to glycol recovery tower, the condensation in first-stage condenser of glycol recovery column overhead gas, uncooled gas enters deep freezer condensation, non-condensable gas goes vacuum system, a phlegma part is through being pumped into trim the top of column, another part delivers to 98% ethylene glycol storage tank as the extraction after cooling of 98% ethylene glycol product, and heavy constituent storage tank delivered to by glycol recovery tower bottoms.
The method of ethylene glycol rectifying in described calcium carbide furnace gas preparing ethylene glycol, at the bottom of methanol distillation column, dehydration tower, dealcoholize column, purifying ethylene glycol tower and ethylene glycol product recovery tower tower, all arrange reboiler, reboiler heat is provided by 1.0 ~ 2.0MPa steam.
The method of ethylene glycol rectifying in described calcium carbide furnace gas preparing ethylene glycol, deep freezer adopts liquefied ammonia as cooling medium.
The method of ethylene glycol rectifying in described calcium carbide furnace gas preparing ethylene glycol, vacuum system is made up of vacuum buffer tank and vacuum pump.
The method of ethylene glycol rectifying in described calcium carbide furnace gas preparing ethylene glycol, after process, ethylene glycol UV transmittance is: 220nm >=85%, 275 nm >=94%, 350 nm >=99.5%.
The method of ethylene glycol rectifying in described calcium carbide furnace gas preparing ethylene glycol, ethylene glycol product purity >=99.98% after process.
According to the difference of the impurity in different times crude product, the crucial equipment for purifying treating tower of ethylene glycol adopts point tower tray charging and a point tower tray side to adopt technology, improves ethylene glycol product purity.Because hydrogenation catalyst synthesizes foreign matter content complexity in thick ethylene glycol, and along with the prolongation in reaction times, side reaction can constantly increase, originally the feed entrance point of tower has departed from original design value, for this increasing the technology of segmentation partial volume charging, adjustment changes the loading tray number of plies and three sections of fractional flow chargings, and the filler quantity of every section in tower is increased, adopt computer software calculate and simulate the rectifying of ethylene glycol simultaneously, optimize the position of draw-off tray, have selected applicable unloading position, the adjustment of load and unloading position can be carried out according to actual motion in actual production,
Complicated in order to solve impurity in thick ethylene glycol, easily form azeotrope, affect the problem of UV transmittance; Learn that foreign matter content is complicated from the above analysis, kind is many, adopts the quality main dealcoholize column and dehydration tower being adopted to the Methods For Purification ethylene glycol rationally mending smart ethylene glycol, and final expection makes product purity reach more than 99.9% level.
Beneficial effect of the present invention: the present invention is according to the difference of the impurity in different times crude product, and ethylene glycol crucial equipment for purifying product tower adopts point tower tray charging and a point tower tray side to adopt technology, improves ethylene glycol product purity; Complicated in order to solve impurity in thick ethylene glycol, easily form azeotrope, affect the problem of UV transmittance, main dealcoholize column and dehydration tower are adopted to the quality of the Methods For Purification ethylene glycol rationally mending smart ethylene glycol, product purity finally can be made to reach more than 99.9% level.The present invention effectively solves China's coal-ethylene glycol poor product quality, share of market is low, can not the difficult problem such as industrialization amplification, have that removal of impurity is high, quality product is high, economical rationality, Technology be feasible, the advantage of safety and stability, the object reducing impurity in product, improve the quality of products can be reached.The present invention can be widely used in, in ethylene glycol distillation technology, being specially adapted in the ethylene glycol rectificating method of calcium carbide furnace gas preparing ethylene glycol.
Accompanying drawing illustrates:
Fig. 1 is process flow sheet of the present invention.
In Fig. 1: 1 be methyl alcohol cooling tower, 2 be preheater, 3 be methanol distillation column, 4 be reboiler, 5 be methanol distillation column return tank, 6 be dehydration tower, 7 be dehydration tower return tank, 8 be dealcoholize column, 9 be purifying ethylene glycol tower, 10 be ethylene glycol product recovery tower, 11 be glycol recovery tower return tank, 12 be one-level water cooler, 13 be deep freezer, 14 be vacuum buffer tank, 15 be vacuum pump, 16 be purifying ethylene glycol tower return tank, 17 be dealcoholize column return tank, 18 for secondary coolers.
Embodiment:
With reference to accompanying drawing 1, the present embodiment comprises the methanol distillation column, dehydration tower, dealcoholize column, purifying ethylene glycol tower and the ethylene glycol product recovery tower that are connected successively, Methanol Recovery column overhead arranges one-level water cooler, secondary coolers, deep freezer, methanol distillation column return tank, vacuum system, dehydration column overhead arranges one-level water cooler, secondary coolers, deep freezer, dehydration tower return tank, vacuum system, dealcoholize column tower top arranges one-level water cooler, deep freezer, dealcoholize column return tank, vacuum system, purifying ethylene glycol column overhead arranges one-level water cooler, deep freezer, purifying ethylene glycol tower return tank, vacuum system, ethylene glycol product recovery tower tower top arranges one-level water cooler, deep freezer, ethylene glycol product recovery tower return tank, vacuum system.
Another embodiment difference is to comprise the steps:
1. the thick ethylene glycol from hydrogenation unit is after preheater and ethylene glycol product heat exchange, enter methanol distillation column bottom, methanol distillation column overhead gas is at one-level water cooler partial condensation, uncooled gas enters secondary condenser condensation, still uncooled gas enters deep freezer, non-condensable gas goes vacuum system, the phlegma of first-stage condenser and secondary condenser enters methanol distillation column return tank through being pumped into methanol distillation column trim the top of column, the phlegma of deep freezer enters front-end volatiles storage tank, methanol distillation column top survey line extraction refined methanol;
2. Methanol Recovery tower reactor liquid is in the middle part of pump delivery to dehydration tower, the condensation in first-stage condenser of dehydration column overhead gas, uncooled gas enters condensation in secondary condenser, still uncooled gas enters deep freezer, non-condensable gas goes vacuum system, the phlegma of first-stage condenser enters dehydration tower return tank through being pumped into dehydration column overhead backflow, and the phlegma of secondary condenser and deep freezer is potato spirit byproduct, enters potato spirit storage tank;
3. dehydrating tower kettle liquid is transported in the middle part of dealcoholize column, the condensation in first-stage condenser of dealcoholize column overhead gas, uncondensed gas sends into condensation in deep freezer, non-condensable gas goes vacuum system, the phlegma of first-stage condenser and deep freezer enters dealcoholize column return tank, phlegma delivers to dealcoholize column trim the top of column through reflux pump, and partial condensation liquid is delivered to lighting end surge tank and stored;
4. dealcoholysis tower bottoms through pump delivery to purifying ethylene glycol tower bottom, the condensation in first-stage condenser of purifying ethylene glycol column overhead gas, uncondensed gas sends into condensation in deep freezer, non-condensable gas goes vacuum system, the phlegma of first-stage condenser and deep freezer enters purifying ethylene glycol tower return tank, a phlegma part is through being pumped into the backflow of purifying ethylene glycol column overhead, and 98% 1 glycol storage tank is delivered in another part extraction;
5. purifying ethylene glycol tower top side take-off premium grads ethylene glycol product, ethylene glycol product after preheater and thick ethylene glycol heat exchange are lowered the temperature again through the laggard ethylene glycol product storage tank of condenser condenses;
6. purifying ethylene glycol tower bottoms is in the middle part of pump delivery to glycol recovery tower, the condensation in first-stage condenser of glycol recovery column overhead gas, uncooled gas enters deep freezer condensation, non-condensable gas goes vacuum system, a phlegma part is through being pumped into trim the top of column, another part delivers to 98% ethylene glycol storage tank as the extraction after cooling of 98% ethylene glycol product, and heavy constituent storage tank delivered to by glycol recovery tower bottoms.
Another embodiment difference is all to arrange reboiler at the bottom of methanol distillation column, dehydration tower, dealcoholize column, purifying ethylene glycol tower and ethylene glycol product recovery tower tower, and reboiler heat is provided by 1.0MPa steam.
Another embodiment difference is all to arrange reboiler at the bottom of methanol distillation column, dehydration tower, dealcoholize column, purifying ethylene glycol tower and ethylene glycol product recovery tower tower, and reboiler heat is provided by 1.5MPa steam.
Another embodiment difference is all to arrange reboiler at the bottom of methanol distillation column, dehydration tower, dealcoholize column, purifying ethylene glycol tower and ethylene glycol product recovery tower tower, and reboiler heat is provided by 2.0MPa steam.
Another embodiment difference is that deep freezer adopts liquefied ammonia as cooling medium.
Another embodiment difference is that vacuum system is made up of vacuum buffer tank and vacuum pump.
Another embodiment difference is that processing rear ethylene glycol UV transmittance is: 220nm 85%, 275 nm 94%, 350 nm 99.5%.
Another embodiment difference is that processing rear ethylene glycol UV transmittance is: 220nm 89%, 275 nm 97%, 350 nm 99.6%.
Another embodiment difference is that processing rear ethylene glycol product purity is 99.98%.
Another embodiment difference is that processing rear ethylene glycol product purity is 99.99%.
Claims (4)
1. the method for ethylene glycol rectifying in calcium carbide furnace gas preparing ethylene glycol, is characterized in that comprising the steps:
1. the thick ethylene glycol from hydrogenation unit is after preheater and ethylene glycol product heat exchange, enter methanol distillation column bottom, methanol distillation column overhead gas is at one-level water cooler partial condensation, uncooled gas enters secondary condenser condensation, still uncooled gas enters deep freezer, non-condensable gas goes vacuum system, the phlegma of first-stage condenser and secondary condenser enters methanol distillation column return tank through being pumped into methanol distillation column trim the top of column, the phlegma of deep freezer enters front-end volatiles storage tank, methanol distillation column top side take-off refined methanol;
2. Methanol Recovery tower reactor liquid is in the middle part of pump delivery to dehydration tower, the condensation in first-stage condenser of dehydration column overhead gas, uncooled gas enters condensation in secondary condenser, still uncooled gas enters deep freezer, non-condensable gas goes vacuum system, the phlegma of first-stage condenser enters dehydration tower return tank through being pumped into dehydration column overhead backflow, and the phlegma of secondary condenser and deep freezer is potato spirit byproduct, enters potato spirit storage tank;
3. dehydrating tower kettle liquid is transported in the middle part of dealcoholize column, the condensation in first-stage condenser of dealcoholize column overhead gas, uncondensed gas sends into condensation in deep freezer, non-condensable gas goes vacuum system, the phlegma of first-stage condenser and deep freezer enters dealcoholize column return tank, phlegma delivers to dealcoholize column trim the top of column through reflux pump, and partial condensation liquid is delivered to lighting end surge tank and stored;
4. dealcoholysis tower bottoms through pump delivery to purifying ethylene glycol tower bottom, the condensation in first-stage condenser of purifying ethylene glycol column overhead gas, uncondensed gas sends into condensation in deep freezer, non-condensable gas goes vacuum system, the phlegma of first-stage condenser and deep freezer enters purifying ethylene glycol tower return tank, a phlegma part is through being pumped into the backflow of purifying ethylene glycol column overhead, and 98% ethylene glycol storage tank is delivered in another part extraction;
5. purifying ethylene glycol tower top side take-off premium grads ethylene glycol product, ethylene glycol product after preheater and thick ethylene glycol heat exchange are lowered the temperature again through the laggard ethylene glycol product storage tank of condenser condenses;
6. purifying ethylene glycol tower bottoms is in the middle part of pump delivery to glycol recovery tower, the condensation in first-stage condenser of glycol recovery column overhead gas, uncooled gas enters deep freezer condensation, non-condensable gas goes vacuum system, a phlegma part is through being pumped into trim the top of column, another part delivers to 98% ethylene glycol storage tank as the extraction after cooling of 98% ethylene glycol product, and heavy constituent storage tank delivered to by glycol recovery tower bottoms;
Gained ethylene glycol product purity >=99.98% after above-mentioned steps process, UV transmittance is: 220nm >=85%, 275nm >=94%, 350nm >=99.5%.
2. the method for ethylene glycol rectifying in calcium carbide furnace gas preparing ethylene glycol according to claim 1, it is characterized in that: at the bottom of methanol distillation column, dehydration tower, dealcoholize column, purifying ethylene glycol tower and ethylene glycol product recovery tower tower, all arrange reboiler, reboiler heat is provided by 1.0 ~ 2.0MPa steam.
3. the method for ethylene glycol rectifying in calcium carbide furnace gas preparing ethylene glycol according to claim 2, is characterized in that: deep freezer adopts liquefied ammonia as cooling medium.
4. the method for ethylene glycol rectifying in calcium carbide furnace gas preparing ethylene glycol according to claim 3, is characterized in that: vacuum system is made up of vacuum buffer tank and vacuum pump.
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Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104725191A (en) * | 2015-03-24 | 2015-06-24 | 中国五环工程有限公司 | Ethylene glycol refining and separating method and system |
| CN106608814B (en) * | 2015-10-22 | 2020-01-03 | 中国石油化工股份有限公司 | Method for improving quality of product of preparing ethylene glycol from synthesis gas |
| CN106946654A (en) * | 2017-03-29 | 2017-07-14 | 东华工程科技股份有限公司 | A kind of separation method of biomass ethylene glycol |
| CN108329193A (en) * | 2018-04-03 | 2018-07-27 | 烟台国邦化工机械科技有限公司 | One kind being used for coal-ethylene glycol industry ethylene glycol recovery process method and system |
| CN109678666A (en) * | 2019-02-22 | 2019-04-26 | 乐陵聚久环保科技有限公司 | A kind of recovery method of synthesis gas preparing ethylene glycol waste liquid |
| CN109939456A (en) * | 2019-04-08 | 2019-06-28 | 宁波中科远东催化工程技术有限公司 | A kind of distillation system and method for coal-ethylene glycol |
| CN109956851B (en) * | 2019-04-08 | 2020-04-07 | 宁波中科远东催化工程技术有限公司 | System and method for rectifying ethylene glycol in preparation of ethylene glycol from synthesis gas |
| CN111592446A (en) * | 2020-06-10 | 2020-08-28 | 东华工程科技股份有限公司 | Rectification system and process for preparing ethylene glycol by dimethyl oxalate hydrogenation |
| CN112062654A (en) * | 2020-08-21 | 2020-12-11 | 陕西聚能新创煤化科技有限公司 | Ethylene glycol rectification system and rectification process |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1319079A (en) * | 1998-09-23 | 2001-10-24 | Basf公司 | Method for producing highly pure monoethylene glycol |
| CN103193595A (en) * | 2013-03-21 | 2013-07-10 | 安徽淮化股份有限公司 | Ethylene glycol rectification device system and rectification technique in industry of producing ethylene glycol by synthesis gas |
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| DE102005004604A1 (en) * | 2005-02-01 | 2006-08-10 | Basf Ag | Method for controlling a hydrogenation |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1319079A (en) * | 1998-09-23 | 2001-10-24 | Basf公司 | Method for producing highly pure monoethylene glycol |
| CN103193595A (en) * | 2013-03-21 | 2013-07-10 | 安徽淮化股份有限公司 | Ethylene glycol rectification device system and rectification technique in industry of producing ethylene glycol by synthesis gas |
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