CN205649877U - Organic waste gas's condensation processing system - Google Patents
Organic waste gas's condensation processing system Download PDFInfo
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- CN205649877U CN205649877U CN201620125095.4U CN201620125095U CN205649877U CN 205649877 U CN205649877 U CN 205649877U CN 201620125095 U CN201620125095 U CN 201620125095U CN 205649877 U CN205649877 U CN 205649877U
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- contact device
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Abstract
The utility model discloses an organic waste gas's condensation processing system, including gas -liquid contact device, with the mechanism of admitting air of gas -liquid contact device's sub -unit connection, with exhaust mechanism, the connection of gas -liquid contact device's upper portion connection gas -liquid contact device's the bottom and the circulation mechanism on upper portion, circulation mechanism includes separator and the refrigerating plant who connects gradually through the circulating line, gas -liquid contact device's centre is equipped with the packing layer, gas -liquid contact device's bottom is equipped with the liquid collecting box, gas -liquid contact device's top is equipped with the defroster. The utility model discloses a condensation processing system, through gas -liquid contact device has realized organic waste gas and coolant liquid direct contact, through its inside packing layer that sets up, has increased area of contact gaseous and liquid to improved heat exchange efficiency and effect, gas and liquid phase have improved cooling efficiency to the flow in the device.
Description
Technical field
This utility model relates to technical field of waste gas treatment, particularly relates to the condensate disposal systems of a kind of organic exhaust gas.
Background technology
Condensation process currently for organic exhaust gas, the overwhelming majority is all to be cooled to close to 0 DEG C by heat exchanger or vaporizer by gas temperature, but typically will not be cooled to less than 0 DEG C, when especially handled organic exhaust gas is very poor with the intermiscibility of water, the problem that organic exhaust gas is condensed to less than the 0 DEG C water vapor condensation frosting arisen that in air.Water vapor condensation frosting can be attached to heat exchanger surface and seriously reduce the heat exchange efficiency of heat exchanger, increases windage, and increasing over time frosting degree can be increasingly severe, and ultimately resulting in processing equipment can not run, even damage equipment.
But, existing condensation process device produces a lot of fogs at exhaust end, it is easy to produces liquid and carries phenomenon secretly, thus has a strong impact on treatment effect；And, gas can be cooled to the processing equipment of less than 0 DEG C at present, its groundwork mode has two kinds: 1, service intermittent, after equipment frosting to a certain extent, stop cooling, equipment carries out the defrosting that heats up, and defrosting terminates to carry out condensing work again, and this planning device can not run continuously, energy consumption high；2, two groups or more condensation process equipment is alternately cooled and defrosts, and this scheme can realize continuous condensation process, but controls complicated, cost height.
Summary of the invention
Technical problem to be solved in the utility model is to provide the condensate disposal systems of a kind of organic exhaust gas, it is possible to realize low energy consumption, the process of low cost, the efficiently organic exhaust gas of cooling.
The condensate disposal systems of organic exhaust gas of the present utility model, it is characterized in that: include gas-liquid contact apparatus, the admission gear being connected with the bottom of described gas-liquid contact apparatus, the exhaust gear being connected with the top of described gas-liquid contact apparatus, connect the bottom of described gas-liquid contact apparatus and the cycling mechanism on top, described cycling mechanism includes segregation apparatus and the refrigerating plant being sequentially connected with by circulating line, the centre of described gas-liquid contact apparatus is provided with packing layer, the bottom of described gas-liquid contact apparatus is provided with liquid collecting box, the top of described gas-liquid contact apparatus is provided with demister.
Further, described admission gear includes pre-filtering device and the pre-cooler being sequentially connected with by admission line.
Further, described exhaust gear includes discharge duct and the cold energy reclamation device being arranged on described discharge duct.
Further, the inlet end on the top of described cycling mechanism is provided with liquid distribution trough.
Further, described segregation apparatus is specially the combination of gravitational separation device or vacuum distillation apparatus or gravitational separation device and vacuum distillation apparatus.
Condensate disposal systems of the present utility model, achieve organic exhaust gas by described gas-liquid contact apparatus directly to contact with coolant, by its internal packing layer arranged, add the contact area of gas and liquid, thus improve heat exchange efficiency and effect, in device, gas flows in opposite directions with liquid, improves cooling effectiveness；Aerofluxus can be carried out except mist by the demister being provided with by the top of described gas-liquid contact apparatus, thus avoid liquid and carry phenomenon secretly, improves treatment effect；The heat energy that can preferentially use refrigerating plant to produce provides thermal source for vacuum distillation apparatus, thus reaches good energy-saving effect；Coolant after released cold quantity can be recycled after cooling again by simple separation, reduces energy consumption and processing cost.
Accompanying drawing explanation
Fig. 1 is the structural representation of the condensate disposal systems that this utility model provides；
Fig. 2 is the structural representation of the embodiment two of the condensate disposal systems that this utility model provides.
As shown in Figure 1, Figure 2, gas-liquid contact apparatus-30, demister-31, liquid distribution trough-32, packing layer-33, gas areal area-34, liquid collecting box-35, admission gear-11, pre-filtering device-10, pre-cooler-20, cycling mechanism-12, segregation apparatus-40, gravitational separation device-41, regulation valve-42, vacuum distillation apparatus-43, densitometer-44, refrigerating plant-50, exhaust gear-13, cold energy reclamation device-60.
Detailed description of the invention
Below in conjunction with the accompanying drawing in this utility model embodiment, the technical scheme in this utility model embodiment is clearly and completely described.
Seeing Fig. 1, be the structural representation of the condensation process device of the organic exhaust gas that this utility model provides, for convenience of description, this figure only provides the structure division relevant with the present invention.
As shown in Figure 1, a kind of condensation process device of organic exhaust gas, including gas-liquid contact apparatus 30, the admission gear 11 being connected with the bottom of described gas-liquid contact apparatus 30, the exhaust gear 13 being connected with the top of described gas-liquid contact apparatus 30, connect the bottom of described gas-liquid contact apparatus 30 and the cycling mechanism 12 on top, described cycling mechanism 12 includes segregation apparatus 40 and the refrigerating plant 50 being sequentially connected with by circulating line (not shown), the centre of described gas-liquid contact apparatus 30 is provided with packing layer 33, the bottom of described gas-liquid contact apparatus 30 is provided with liquid collecting box 35, the top of described gas-liquid contact apparatus 30 is provided with demister 31, described demister 31 can effectively prevent liquid from carrying secretly.
Concrete, described admission gear 11 includes pre-filtering device 10 and the pre-cooler 20 being sequentially connected with by admission line (not shown).
Concrete, described exhaust gear 13 includes discharge duct (not shown) and the cold energy reclamation device 60 being arranged on described discharge duct.
Further improvement as technique scheme, the inlet end on the top of described cycling mechanism 12 is provided with liquid distribution trough 32, coolant can be divided equally by described liquid distribution trough 32, so that coolant can be impregnated with described packing layer 33 uniformly, improves cooling effect.
Concrete, described segregation apparatus 40 is specially the combination of gravitational separation device 41 or vacuum distillation apparatus 43 or gravitational separation device 41 and vacuum distillation apparatus 43.
Embodiment one
Above-mentioned condensation process device is utilized to process the organic exhaust gas containing ethyl acetate
First, determine that the target chilling temperature of the pending waste gas containing ethyl acetate is-25 DEG C, and determine the physical characteristic of ethyl acetate；Secondly, according to physical characteristics such as the freezing point of ethyl acetate, boiling points, selecting the glycol water of 50%VOL as coolant, wherein, the freezing point of the glycol water of described glycol water is-38 DEG C；Then, glycol water is cooled to-30 DEG C through refrigerating plant 50, sprayed from the top down of gas-liquid contact apparatus 30 equably by the liquid distribution trough 32 on cycling mechanism 12 top, glycol water flows down through packing layer 33 homogeneous immersion packing layer 33, in last influent collecting box 35；Then, organic exhaust gas containing ethyl acetate is carried out filtering and impurity removing by pre-filtering device 10, after being cooled to 0 DEG C-5 DEG C by pre-cooler 20 again, enter from the admission gear 11 of the bottom of gas-liquid contact apparatus 30, after the gas areal area 34 in gas-liquid contact apparatus 30 is uniformly distributed, discharge from exhaust gear 13 after being drawn past packing layer 33 by blower fan, period, organic exhaust gas containing ethyl acetate carries out sufficient gas-to-liquid contact with the glycol water of distribution on packing layer 33, realize heat exchange, during glycol water flows downward, temperature gradually rises, during organic exhaust gas flows up, temperature is gradually lowered and is condensed out ethyl acetate and water, condensed fluid mixes with glycol water；Mixing liquid is flowed downward by self gravitation effect, is collected by liquid collecting box 35；Again the mixture of the ethylene glycol in liquid collecting box 35, water and ethyl acetate is carried out simple separation by segregation apparatus 40；Finally, the top returning gas-liquid contact apparatus 30 after being freezed by glycol water isolated in above-mentioned steps recycles.
Concrete, owing to ethyl acetate dissolubility in water and ethylene glycol is smaller, so first passing through the isolated upper liquid of gravitational separation device 41 is ethyl acetate, glycol water that subnatant mainly dilutes and a small amount of ethyl acetate of dissolving；Owing to the boiling point of ethylene glycol is far above water and ethyl acetate, so again by distillation of simply reducing pressure, distilling out ethyl acetate and the part water of dissolving, making the concentration of glycol water return to 50%VOL, wherein, the liquid that slips out of ethyl acetate and water can separating-purifying further.
Preferably, the thermal source needed for described vacuum distillation apparatus 43 can be low-grade cheap thermal source, the heat energy that the preferential condenser using described refrigerating plant 50 produces.
Preferably, the cryogenic gas after condensation process can be warming up to be then discharged out close to ambient temperature after cold energy reclamation device 60 reclaims cold.
Embodiment two
Above-mentioned processing means is utilized to process the organic exhaust gas containing D40 solvent naphtha
D40 solvent naphtha is widely used in industrial cleaning agent, and such as aluminium foil cleaning etc., the waste gas containing D40 solvent naphtha that general aluminium foil cleaning line is discharged, after the condensation process of-25 DEG C, can reclaim the D40 solvent naphtha of more than 95%, and the solvent naphtha content in waste gas is the most few.
During process, first, determine that the target chilling temperature of the pending waste gas containing D40 solvent naphtha is-25 DEG C, and determine the physical characteristic of D40 solvent naphtha；Secondly, according to physical characteristics such as the freezing point of D40 solvent naphtha, boiling points, selecting the glycol water of 50%VOL as coolant, wherein, the freezing point of the glycol water of described glycol water is-38 DEG C；Then, glycol water is cooled to-30 DEG C through refrigerating plant 50, sprayed from the top down of gas-liquid contact apparatus 30 equably by the liquid distribution trough 32 on cycling mechanism 12 top, glycol water flows down through packing layer 33 homogeneous immersion packing layer 33, in last influent collecting box 35；Then, organic exhaust gas containing D40 solvent naphtha is carried out filtering and impurity removing by pre-filtering device 10, after being cooled to 0 DEG C-5 DEG C by pre-cooler 20 again, enter from the admission gear 11 of the bottom of gas-liquid contact apparatus 30, after the gas areal area 34 in gas-liquid contact apparatus 30 is uniformly distributed, discharge from exhaust gear 13 after being drawn past packing layer 33 by blower fan, period, organic exhaust gas containing D40 solvent naphtha carries out sufficient gas-to-liquid contact with the glycol water of distribution on packing layer 33, realize heat exchange, during glycol water flows downward, temperature gradually rises, during organic exhaust gas flows up, temperature is gradually lowered and is condensed out D40 solvent naphtha and water, condensed fluid mixes with glycol water；Mixing liquid is flowed downward by self gravitation effect, collects this mixing liquid by liquid collecting box 35；Again the mixture of the ethylene glycol in liquid collecting box 35, water and D40 solvent naphtha is carried out simple separation by segregation apparatus 40；Finally, the top returning gas-liquid contact apparatus 30 after being freezed by isolated glycol water recycles.
Concrete, owing to D40 solvent naphtha can not be dissolved in water or ethylene glycol, so first passing through the isolated upper liquid of gravitational separation device 41 is D40 solvent naphtha, the glycol water that subnatant is mainly mixed with the condensed water in waste gas and dilutes, then subnatant is distributed and be partly into vacuum distillation apparatus 43 and process, due to ethylene glycol boiling point far above water and with water not azeotropic, therefore fractional distillation water outlet, glycol water after being concentrated, glycol water after concentrating again mixes with the subnatant not shunted, the concentration of mixed glycol water is detected by the densitometer 44 on cycling mechanism 12, the flow of the glycol water after being concentrated by regulation valve 42 regulation, the concentration of mixed liquor is adjusted to about 50%VOL.
Preferably, the thermal source needed for described vacuum distillation apparatus 43 can be low-grade cheap thermal source, the heat energy that the preferential condenser using described refrigerating plant 50 produces.
Preferably, the cryogenic gas after condensation process can be warming up to be then discharged out close to ambient temperature after cold energy reclamation device 60 reclaims cold.
The above is preferred implementation of the present utility model; it should be pointed out that, for those skilled in the art, on the premise of without departing from this utility model principle; can also make some improvements and modifications, these improvements and modifications are also considered as protection domain of the present utility model.
Claims (5)
1. the condensate disposal systems of an organic exhaust gas, exhaust gear that the admission gear being connected with the bottom of described gas-liquid contact apparatus including gas-liquid contact apparatus is connected with the top of described gas-liquid contact apparatus, connect the bottom of described gas-liquid contact apparatus and the cycling mechanism on top, described cycling mechanism includes segregation apparatus and the refrigerating plant being sequentially connected with by circulating line, the centre of described gas-liquid contact apparatus is provided with packing layer, the bottom of described gas-liquid contact apparatus is provided with liquid collecting box, and the top of described gas-liquid contact apparatus is provided with demister.
Processing system the most according to claim 1, it is characterised in that: described admission gear includes pre-filtering device and the pre-cooler being sequentially connected with by admission line.
Processing system the most according to claim 1, it is characterised in that: described exhaust gear includes discharge duct and the cold energy reclamation device being arranged on described discharge duct.
Processing system the most according to claim 1, it is characterised in that: the inlet end on the top of described cycling mechanism is provided with liquid distribution trough.
Processing system the most according to claim 1, it is characterised in that: described segregation apparatus is specially the combination of gravitational separation device or vacuum distillation apparatus or gravitational separation device and vacuum distillation apparatus.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620125095.4U CN205649877U (en) | 2016-02-17 | 2016-02-17 | Organic waste gas's condensation processing system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620125095.4U CN205649877U (en) | 2016-02-17 | 2016-02-17 | Organic waste gas's condensation processing system |
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| CN205649877U true CN205649877U (en) | 2016-10-19 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201620125095.4U Expired - Fee Related CN205649877U (en) | 2016-02-17 | 2016-02-17 | Organic waste gas's condensation processing system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109999528A (en) * | 2019-04-18 | 2019-07-12 | 中国科学院山西煤炭化学研究所 | Exhaust treatment system |
| CN110147128A (en) * | 2019-06-11 | 2019-08-20 | 广东环葆嘉节能科技有限公司 | A kind of temprature control method and device |
-
2016
- 2016-02-17 CN CN201620125095.4U patent/CN205649877U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109999528A (en) * | 2019-04-18 | 2019-07-12 | 中国科学院山西煤炭化学研究所 | Exhaust treatment system |
| CN110147128A (en) * | 2019-06-11 | 2019-08-20 | 广东环葆嘉节能科技有限公司 | A kind of temprature control method and device |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20161019 Termination date: 20210217 |
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| CF01 | Termination of patent right due to non-payment of annual fee |