CN105669380A - Ethylene glycol recovery device of polyester wastewater recovery system and ethylene glycol recovery method - Google Patents
Ethylene glycol recovery device of polyester wastewater recovery system and ethylene glycol recovery method Download PDFInfo
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- CN105669380A CN105669380A CN201610151943.3A CN201610151943A CN105669380A CN 105669380 A CN105669380 A CN 105669380A CN 201610151943 A CN201610151943 A CN 201610151943A CN 105669380 A CN105669380 A CN 105669380A
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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
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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
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Abstract
The invention relates to an ethylene glycol recovery device of a polyester wastewater recovery system. The ethylene glycol recovery device of the polyester wastewater recovery system is characterized by comprising a primary-effect heater (1), a primary-effect gas-liquid separator (2), a secondary-effect heater (3), a secondary-effect gas-liquid separator (4), a tertiary-effect heater (5), a tertiary-effect gas-liquid separator (6), a first-stage condenser (7), a second-stage condenser (8), a heat exchanger (10) and an ethylene glycol rectifying tower (11). The ethylene glycol recovery device of the polyester wastewater recovery system has the advantages of being low in energy consumption, high in product quality and good in equipment use stability.
Description
Technical field
The present invention relates to the glycol recovery device of a kind of polyester waste water recovery system and glycol recovery method.
Background technology
The production domestic enterprise of polyester (PET) generally adopts taking terephthalic acid and ethylene glycol as the direct esterification method of raw material, and in its esterification step production process, the concentration of the waste water chemical oxygen demand cod of discharge is between 18000-40000mg/L. Mainly containing organic pollutants in waste water is ethylene glycol, acetaldehyde and heterocycle organism, and wherein volatile components acetaldehyde accounts for about the 50% of total organic pollutant. At present, international and domestic traditional technology adopts air lift method process esterification waste water, and the waste gas after air lift is delivered to roasting kiln and burned, it is possible to save part fuel. COD value of waste water after air lift drops to below 5000mg/L, subsequent wastewater treatment operation mainly adopts anaerobic and aerobic process, owing to aldehyde material toxicity is very big, it is unfavorable for bacterial growth, cause biochemical method processing efficiency lower, and the waste water for high cod values, if adopting separately Biochemical method, not only investment cost height but also processing cost are also very expensive.
Chinese patent 201410107610.1 discloses the system reclaiming acetaldehyde and ethylene glycol in a kind of polyester waste water, and ethylene glycol directly enters ethylene glycol rectifying tower after being separated with acetaldehyde and purifies, and adopts in the process directly purified and has three place's defects:
1, energy consumption is higher: monoethylene glycol distillation tower calculates with charging amount 3.5T/h, thermal oil demand 1800KW/h(temperature about 180 DEG C, flow 140m3About/h), energy consumption is higher.
2, the ethylene glycol quality of finished reclaimed is poor: the temperature for the thermal oil of heat exchange is higher, the organism such as part ethylene glycol and heterocycle is subject to high temperature and there will be chemical reaction in the process, ethylene glycol is caused to start jaundice, ethylene glycol finished product colour (b value) > 6, recovering effect is deteriorated, and production of polyester stability is had impact by the ethylene glycol after recovery.
3, equipment impact is big: due to heat-conducting oil heating temperature height, ethylene glycol and other organism at high temperature easily form the bigger polymkeric substance of viscosity, are attached on tower packing, and equipment to be cleaned after running for some time, device must stop, and brings instability to system.
Therefore seek that a kind of energy consumption is low, the glycol recovery device of the polyester waste water recovery system of quality product height, equipment use good stability is particularly important.
Summary of the invention
It is an object of the invention to overcome above-mentioned deficiency, it is provided that a kind of energy consumption is low, the glycol recovery device of the polyester waste water recovery system of quality product height, equipment use good stability.
The object of the present invention is achieved like this:
A glycol recovery device for polyester waste water recovery system, it comprises an effect well heater, an effect gas-liquid separator, two effect well heaters, two effect gas-liquid separators, three effect well heaters, three effect gas-liquid separators, first-stage condenser, secondary condenser, interchanger and ethylene glycol rectifying tower;
Wherein lead in an effect well heater and imitate heat medium pipe road into one one, the its top feed mouth of one effect well heater leads to imitates well heater feed-pipe into one one, the hypomere of one effect well heater is connected with the hypomere of an effect gas-liquid separator, one effect gas-liquid separator top by two effect well heater vapour pipes be connected two effect well heaters upper section, the discharge gate of the bottom of one effect gas-liquid separator imitates, through one two, its top feed mouth that well heater feed-pipe is communicated to two effect well heaters, the hypomere of two effect well heaters is connected with the hypomere of two effect gas-liquid separators, two effect gas-liquid separators tops by three effect well heater vapour pipes be connected three effect well heaters upper section, the discharge gate of the bottom of two effect gas-liquid separators imitates, through one three, its top feed mouth that well heater feed-pipe is communicated to three effect well heaters, the hypomere of three effect well heaters is connected with the hypomere of three effect gas-liquid separators, the discharge gate of the bottom of three effect gas-liquid separators is communicated to interchanger through an interchanger feed-pipe, the top of three effect gas-liquid separators is connected first-stage condenser by first-stage condenser steam pipeline, the phlegma that first-stage condenser is discharged leads to secondary condenser, ethylene glycol rectifying tower feed-pipe it is communicated with between described interchanger and ethylene glycol rectifying tower, lead to into an ethylene glycol rectifying tower heat medium pipe road in ethylene glycol rectifying tower, the top of ethylene glycol rectifying tower has connected a mixed vapour discharge line, the bottom of ethylene glycol rectifying tower connects an ethylene glycol discharge line, ethylene glycol discharge line connects finished pot after interchanger,
The glycol recovery device of a kind of polyester waste water recovery system, it also comprises negative-pressure vacuum producer, the one-level that negative-pressure vacuum producer connects vacuumizes pipeline and is connected to secondary condenser, secondary condenser connects two grades again and vacuumizes pipeline, two grades vacuumize pipeline and separate and branched be connected to first-stage condenser steam pipeline respectively, three effect well heaters upper section, stage casing and hypomere, the hypomere of three effect well heaters also connects three grades and vacuumizes pipeline, three grades vacuumize pipeline and connect to separate and branched be connected to three effect well heater feed-pipes respectively, two effect well heaters upper section, stage casing and hypomere.
Wherein three grades vacuumize pipeline by an intermediate condensation tank.
A glycol recovery method for the glycol recovery device of polyester waste water recovery system, adopts the glycol recovery device of above-mentioned a kind of polyester waste water recovery system to carry out operation, and the step of this glycol recovery method is as follows:
Ethylene glycol forms mixed solution in the middle of one-level with acetaldehyde after being separated, in the middle of one-level, the glycol concentration of mixed solution is 8% ~ 10%, one effect heat medium pipe Dao Neitong enters the thermal oil of 160 ~ 170 DEG C, pressure in one effect well heater is-0.03MPa, one effect well heater and two steam temperatures imitated in well heater feed-pipes are 90 DEG C ~ 95 DEG C, in the middle of in two effect well heater feed-pipes two grades, the glycol concentration of mixed solution is 20% ~ 25%, pressure in two effect well heaters is-0.05MPa, two effect well heaters and three steam temperatures imitated in well heater feed-pipes are 85 DEG C ~ 90 DEG C, in the middle of in three effect well heater feed-pipes three grades, the glycol concentration of mixed solution is 40% ~ 50%, pressure in three effect well heaters is-0.085MPa, three steam temperatures imitated in well heaters and first-stage condenser steam pipeline are 80 DEG C ~ 85 DEG C, in the middle of level Four in interchanger feed-pipe, the glycol concentration of mixed solution is 80% ~ 85%, in the middle of level Four, mixeding liquid temperature is 70 DEG C ~ 80 DEG C, in the middle of level Four, mixed solution is promoted to 85 DEG C ~ 95 DEG C through the heat-exchange temperature of interchanger, the glycol concentration that in the middle of level Four, mixed solution carries out the finished fluid of discharge after rectifying through ethylene glycol rectifying tower is 90% ~ 95%, finished fluid is 115 DEG C ~ 120 DEG C in the temperature before interchanger, finished fluid temperature after mixed solution heat exchange in the middle of interchanger and level Four is 85 DEG C ~ 95 DEG C, pressure in ethylene glycol rectifying tower is-0.08MPa, the thermal oil temperature in the ethylene glycol rectifying tower heat medium pipe road in ethylene glycol rectifying tower is 160 ~ 170 DEG C.
Compared with prior art, the invention has the beneficial effects as follows:
1, energy consumption saving
Thermal oil demand 600KW/h(temperature 150 DEG C ~ 170 DEG C, flow 110m3About/h), mainly recycle the steam after multiple-effect.
2, the ethylene glycol quality of finished reclaimed promotes
Ethylene glycol finished product colour (b value) < 5, on production of polyester substantially without impact after reuse.
3, the impact of equipment is little
Owing to Heating temperature is lower, form polymkeric substance probability and greatly reduce, it is not easy to stick equipment, run to device long-term stability and provide guarantee.
The present invention adopts the multiple-effect evaporation of particular design in conjunction with the ethylene glycol in negative pressure rectification process purification waste water, and multi-effect evaporating device of the present invention effect number is 3 ~ 4 effects. Adopting low temperature heat-conducting oil system as the thermal source of an effect, follow-up well heater imitates the steam of evaporation as thermal source before all adopting. Simultaneously, consider the problem adopting separately multiple-effect evaporation technique that the COD value in lime set waste water may be caused higher, after ethylene glycol purity is purified to 80% ~ 85% by 8% ~ 10%, then adopt negative pressure rectifying that ethylene glycol is purified to 90% ~ 95%, thus reach energy-conservation and promote the quality of reuse ethylene glycol. Therefore the glycol recovery device of polyester waste water recovery system of the present invention has that energy consumption is low, the advantage of quality product height, equipment use good stability.
Accompanying drawing explanation
Fig. 1 is the structural representation of the present invention.
Wherein:
One effect well heater 1, is imitated well heater feed-pipe 1.1, and is imitated heat medium pipe road 1.2
One effect gas-liquid separator 2,
Two effect well heaters 3, two are imitated well heater feed-pipe 3.1, two and are imitated well heater vapour pipe 3.2
Two effect gas-liquid separators 4,
Three effect well heaters 5, three are imitated well heater feed-pipe 5.1, three effect well heater vapour pipe 5.2, three grades and are vacuumized pipeline 5.3
Three effect gas-liquid separators 6,
First-stage condenser 7, first-stage condenser steam pipeline 7.1
Secondary condenser 8, two grades vacuumizes pipeline 8.1
Negative-pressure vacuum producer 9, one-level vacuumize pipeline 9.1
Interchanger 10, interchanger feed-pipe 10.1
Ethylene glycol rectifying tower 11, ethylene glycol rectifying tower feed-pipe 11.1, ethylene glycol rectifying tower heat medium pipe road 11.2, mixed vapour discharge line 11.3, ethylene glycol discharge line 11.4.
Embodiment
See Fig. 1, the glycol recovery device of a kind of polyester waste water recovery system that the present invention relates to, it comprises an effect well heater 1, and imitates gas-liquid separator 2, two effect well heater 3, two effect gas-liquid separator 4, three effect well heater 5, three effect gas-liquid separator 6, first-stage condenser 7, secondary condenser 8, negative-pressure vacuum producer 9, interchanger 10 and ethylene glycol rectifying tower 11.
Wherein lead to the effect heat medium pipe road 1.2 into a bottom in and top out in an effect well heater 1, the its top feed mouth of one effect well heater 1 leads to imitates well heater feed-pipe 1.1 into one one, the material that one effect heat medium pipe road 1.2 is entered by an effect well heater feed-pipe 1.1 for heating in an effect well heater 1, the hypomere of one effect well heater 1 is connected with the hypomere of an effect gas-liquid separator 2, one effect gas-liquid separator 2 top by two effect well heater vapour pipes 3.2 be connected two effect well heaters 3 upper section, then the discharge gate of the discharge gate of the bottom of one effect well heater 1 and the bottom of an effect gas-liquid separator 2 collects imitates, through one two, its top feed mouth that well heater feed-pipe 3.1 is communicated to two effect well heaters 3, the material that steam in two effect well heater vapour pipes 3.2 is entered by two effect well heater feed-pipes 3.1 for heating in two effect well heaters 3, the hypomere of two effect well heaters 3 is connected with the hypomere of two effect gas-liquid separators 4, two effect gas-liquid separators 4 top by three effect well heater vapour pipes 5.2 be connected three effect well heaters 5 upper section, then the discharge gate of the discharge gate of the bottom of two effect well heaters 3 and the bottom of two effect gas-liquid separators 4 collects imitates, through one three, its top feed mouth that well heater feed-pipe 5.1 is communicated to three effect well heaters 5, the material that steam in three effect well heater vapour pipes 5.2 is entered by three effect well heater feed-pipes 5.1 for heating in three effect well heaters 5, the hypomere of three effect well heaters 5 is connected with the hypomere of three effect gas-liquid separators 6, the discharge gates of the bottom of three effect well heaters 5 collect with three discharge gates of bottom imitating gas-liquid separators 6 and are then communicated to interchanger 10 through an interchanger feed-pipe 10.1, the top of three effect gas-liquid separators 5 is connected first-stage condenser 7 by first-stage condenser steam pipeline 7.1, first-stage condenser 7 is horizontal condenser, the phlegma that first-stage condenser 7 is discharged leads to secondary condenser 8, secondary condenser 8 is vertical (type) condenser, vertical (type) condenser can be arranged in series multiple stage, water in secondary condenser 8 is extracted out reuse by vacuum pump.Ethylene glycol rectifying tower feed-pipe 11.1 it is communicated with between described interchanger 10 and ethylene glycol rectifying tower 11, the ethylene glycol rectifying tower heat medium pipe road 11.2 into a bottom in and top out is led in ethylene glycol rectifying tower 11, the top of ethylene glycol rectifying tower 11 has connected a mixed vapour discharge line 11.3, the bottom of ethylene glycol rectifying tower 11 connects an ethylene glycol discharge line 11.4, and ethylene glycol discharge line 11.4 connects finished pot after interchanger 10. negative-pressure vacuum producer 9 can be arranged in parallel two, the one-level that negative-pressure vacuum producer 9 connects vacuumizes pipeline 9.1 and is connected to secondary condenser 8, secondary condenser 8 connects two grades again and vacuumizes pipeline 8.1, two grades vacuumize pipeline 8.1 and separate and branched be connected to first-stage condenser steam pipeline 7.1 respectively, three effect well heaters 5 upper section, stage casing and hypomere, the hypomere of three effect well heaters 5 also connects three grades and vacuumizes pipeline 5.3, three grades vacuumize pipeline 5.3 and connect to separate and branched be connected to three effect well heater feed-pipes 5.1 respectively, two effect well heaters 3 upper section, stage casing and hypomere, wherein three grades vacuumize pipeline 5.3 by an intermediate condensation tank 12. first-stage condenser 7 and negative-pressure vacuum producer 9 are cooled by cooling water circulation pipeline.
The glycol recovery method of the glycol recovery device of a kind of polyester waste water recovery system:
Ethylene glycol forms mixed solution in the middle of one-level with acetaldehyde after being separated, in the middle of one-level, the glycol concentration of mixed solution is 8% ~ 10%, in the middle of one-level, mixed solution enters an effect well heater 1 through an effect well heater feed-pipe 1.1, the thermal oil into 160 ~ 170 DEG C is led in one effect heat medium pipe road 1.2, middle mixed solution enters an effect gas-liquid separator 2 after the heating in an effect heat medium pipe road 1.2 and carries out aqueous vapor separation, pressure in one effect well heater 1 is-0.03MPa, one effect well heater 1 and two steam temperatures imitated in well heater feed-pipes 3.1 are 90 DEG C ~ 95 DEG C, in the middle of in two effect well heater feed-pipes 3.1 two grades, the glycol concentration of mixed solution is 20% ~ 25%, then two grades of middle mixed solutions enter two effect well heaters 3 through two effect well heater feed-pipes 3.1, pressure in two effect well heaters 3 is-0.05MPa, two effect well heaters 3 and three steam temperatures imitated in well heater feed-pipes 5.1 are 85 DEG C ~ 90 DEG C, in the middle of in three effect well heater feed-pipes 5.1 three grades, the glycol concentration of mixed solution is 40% ~ 50%, then three grades of middle mixed solutions enter three effect well heaters 5 through three effect well heater feed-pipes 5.1, pressure in three effect well heaters 5 is-0.085MPa, three steam temperatures imitated in well heaters 5 and first-stage condenser steam pipeline 7.1 are 80 DEG C ~ 85 DEG C, in the middle of level Four in interchanger feed-pipe 10.1, the glycol concentration of mixed solution is 80% ~ 85%, in the middle of level Four, mixeding liquid temperature is 70 DEG C ~ 80 DEG C, in the middle of level Four, mixed solution is promoted to 85 DEG C ~ 95 DEG C through the heat-exchange temperature of interchanger 10, in the middle of level Four, the glycol concentration of the finished fluid that mixed solution is discharged after ethylene glycol rectifying tower 11 carries out rectifying is 90% ~ 95%, finished fluid is 115 DEG C ~ 120 DEG C in the temperature before interchanger 10, finished fluid temperature after mixed solution heat exchange in the middle of interchanger 10 with level Four is 85 DEG C ~ 95 DEG C, pressure in ethylene glycol rectifying tower 11 is-0.08MPa, the thermal oil temperature in the ethylene glycol rectifying tower heat medium pipe road 11.2 in ethylene glycol rectifying tower 11 is 160 ~ 170 DEG C.
Imitate due to each effect well heater 1, two in well heater 3 and three effect well heaters 5 and all there is negative pressure, the water vapour boiling point of corresponding position is reduced, it is easy to form water vapour, and one effect well heater 1, two imitate well heater 3 and three effect well heaters 5 become far away gradually owing to leaving negative-pressure vacuum producer 9, the negative pressure that one effect well heater 1, two imitates well heater 3 and three effect well heaters 5 formation is increased gradually, therefore the water vapour boiling point of corresponding position reduces gradually, the heating that the water vapour that the temperature in front road is relatively high can be used in lower road uses, and improves energy utilization rate.
Claims (4)
1. the glycol recovery device of a polyester waste water recovery system, it is characterised in that it comprises an effect well heater (1), effect gas-liquid separator (2), two effects well heater (3), two effects gas-liquid separator (4), three effects well heater (5), three effects gas-liquid separator (6), first-stage condenser (7), secondary condenser (8), interchanger (10) and ethylene glycol rectifying tower (11);
Wherein lead in effect well heater (1) and imitate heat medium pipe road (1.2) into one one, the its top feed mouth of one effect well heater (1) leads to imitates well heater feed-pipe (1.1) into one one, the hypomere of one effect well heater (1) is connected with the hypomere of effect gas-liquid separator (2), one effect gas-liquid separator (2) top by two effect well heater vapour pipe (3.2) be connected two effect well heater (3) upper section, the discharge gate of the bottom of one effect gas-liquid separator (2) imitates, through one two, its top feed mouth that well heater feed-pipe (3.1) is communicated to two effect well heaters (3), the hypomere of two effects well heater (3) is connected with the hypomere of two effects gas-liquid separator (4), two effect gas-liquid separator (4) tops by three effect well heater vapour pipe (5.2) be connected three effect well heater (5) upper section, the discharge gate of the bottom of two effects gas-liquid separator (4) imitates, through one three, its top feed mouth that well heater feed-pipe (5.1) is communicated to three effect well heaters (5), the hypomere of three effects well heater (5) is connected with the hypomere of three effects gas-liquid separator (6), the discharge gate of the bottom of three effects gas-liquid separator (6) is communicated to interchanger (10) through an interchanger feed-pipe (10.1), the top of three effects gas-liquid separator (5) is connected first-stage condenser (7) by first-stage condenser steam pipeline (7.1), the phlegma that first-stage condenser (7) is discharged leads to secondary condenser (8), ethylene glycol rectifying tower feed-pipe (11.1) it is communicated with between described interchanger (10) and ethylene glycol rectifying tower (11), lead to into ethylene glycol rectifying tower heat medium pipe road (11.2) in ethylene glycol rectifying tower (11), the top of ethylene glycol rectifying tower (11) has connected a mixed vapour discharge line (11.3), the bottom of ethylene glycol rectifying tower (11) connects an ethylene glycol discharge line (11.4), ethylene glycol discharge line (11.4) connects finished pot after interchanger (10).
2. the glycol recovery device of a kind of polyester waste water recovery system according to claim 1, it also comprises negative-pressure vacuum producer (9), the one-level that negative-pressure vacuum producer (9) connects vacuumizes pipeline (9.1) and is connected to secondary condenser (8), secondary condenser (8) connects two grades again and vacuumizes pipeline (8.1), two grades vacuumize pipeline (8.1) and separate and branched be connected to first-stage condenser steam pipeline (7.1) respectively, three effect well heater (5) upper section, stage casing and hypomere, the hypomere of three effects well heater (5) also connects three grades and vacuumizes pipeline (5.3), three grades vacuumize pipeline (5.3) and connect to separate and branched be connected to three effects well heater feed-pipe (5.1) respectively, two effect well heater (3) upper section, stage casing and hypomere.
3. the glycol recovery device of a kind of polyester waste water recovery system according to claim 2, it is characterised in that wherein three grades vacuumize pipeline (5.3) by an intermediate condensation tank (12).
4. the glycol recovery method of the glycol recovery device of a polyester waste water recovery system, it is characterised in that adopting the glycol recovery device of a kind of polyester waste water recovery system as claimed in claim 1 to carry out operation, the step of this glycol recovery method is as follows:
Ethylene glycol forms mixed solution in the middle of one-level with acetaldehyde after being separated, in the middle of one-level, the glycol concentration of mixed solution is 8% ~ 10%, one effect heat medium pipe Dao Neitong enters the thermal oil of 160 ~ 170 DEG C, pressure in one effect well heater is-0.03MPa, one effect well heater and two steam temperatures imitated in well heater feed-pipes are 90 DEG C ~ 95 DEG C, in the middle of in two effect well heater feed-pipes two grades, the glycol concentration of mixed solution is 20% ~ 25%, pressure in two effect well heaters is-0.05MPa, two effect well heaters and three steam temperatures imitated in well heater feed-pipes are 85 DEG C ~ 90 DEG C, in the middle of in three effect well heater feed-pipes three grades, the glycol concentration of mixed solution is 40% ~ 50%, pressure in three effect well heaters is-0.085MPa, three steam temperatures imitated in well heaters and first-stage condenser steam pipeline are 80 DEG C ~ 85 DEG C, in the middle of level Four in interchanger feed-pipe, the glycol concentration of mixed solution is 80% ~ 85%, in the middle of level Four, mixeding liquid temperature is 70 DEG C ~ 80 DEG C, in the middle of level Four, mixed solution is promoted to 85 DEG C ~ 95 DEG C through the heat-exchange temperature of interchanger, the glycol concentration that in the middle of level Four, mixed solution carries out the finished fluid of discharge after rectifying through ethylene glycol rectifying tower is 90% ~ 95%, finished fluid is 115 DEG C ~ 120 DEG C in the temperature before interchanger, finished fluid temperature after mixed solution heat exchange in the middle of interchanger and level Four is 85 DEG C ~ 95 DEG C, pressure in ethylene glycol rectifying tower is-0.08MPa, the thermal oil temperature in the ethylene glycol rectifying tower heat medium pipe road in ethylene glycol rectifying tower is 160 ~ 170 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610151943.3A CN105669380B (en) | 2016-03-17 | 2016-03-17 | The ethylene glycol recyclable device and ethylene glycol recovery method of polyester waste water recovery system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610151943.3A CN105669380B (en) | 2016-03-17 | 2016-03-17 | The ethylene glycol recyclable device and ethylene glycol recovery method of polyester waste water recovery system |
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| Publication Number | Publication Date |
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| CN105669380A true CN105669380A (en) | 2016-06-15 |
| CN105669380B CN105669380B (en) | 2018-12-11 |
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| CN201610151943.3A Expired - Fee Related CN105669380B (en) | 2016-03-17 | 2016-03-17 | The ethylene glycol recyclable device and ethylene glycol recovery method of polyester waste water recovery system |
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| CN113461488A (en) * | 2021-07-30 | 2021-10-01 | 重庆万凯新材料科技有限公司 | Ethylene glycol circulating treatment process |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109179542A (en) * | 2018-11-13 | 2019-01-11 | 重庆华峰化工有限公司 | Ethylene glycol, the Distallation systm of diethylene glycol and distillation technique in polyalcohol waste liquid |
| CN109179542B (en) * | 2018-11-13 | 2023-11-24 | 重庆华峰化工有限公司 | Distillation system and distillation process for glycol and diethylene glycol in polyol waste liquid |
| CN113461488A (en) * | 2021-07-30 | 2021-10-01 | 重庆万凯新材料科技有限公司 | Ethylene glycol circulating treatment process |
| CN113461488B (en) * | 2021-07-30 | 2023-06-02 | 重庆万凯新材料科技有限公司 | Ethylene glycol circulation treatment process |
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| Publication number | Publication date |
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| CN105669380B (en) | 2018-12-11 |
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