CN101962813A - Thermal-energy recycling system in spandex-spinning production process - Google Patents
Thermal-energy recycling system in spandex-spinning production process Download PDFInfo
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- CN101962813A CN101962813A CN201010254846XA CN201010254846A CN101962813A CN 101962813 A CN101962813 A CN 101962813A CN 201010254846X A CN201010254846X A CN 201010254846XA CN 201010254846 A CN201010254846 A CN 201010254846A CN 101962813 A CN101962813 A CN 101962813A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/50—Manufacturing or production processes characterised by the final manufactured product
- Y02P70/62—Manufacturing or production processes characterised by the final manufactured product related technologies for production or treatment of textile or flexible materials or products thereof, including footwear
Abstract
The invention relates to a thermal-energy recycling system in a spandex-spinning production process, which is used for recycling the thermal energy in the spandex-spinning production process, comprises a spinning shaft (1), a first wind pipe (2), a solvent recovering system (3), a heating-medium heater (4), a second wind pipe (5) and a heating-medium or electric heater (6) and is characterized in that heat-pipe heat exchangers are provided with two stages or more than two stages, the two stages or more than two stage of heat-pipe heat exchangers are sequentially connected in series, working media with different boiling points are filled in each stage of heat-pipe heat exchanger, and the boiling points of the working media filled in each stage of heat-pipe heat exchanger are sequentially decreased under normal pressure. In the invention, a traditional first-stage heat-pipe heat exchanger is changed into the two stages or more than two stage of heat-pipe heat exchangers, and the working media with different boiling points are used for replacing original demineralized water, so that the gas temperature at the hot side of the heat-pipe heat exchangers is further decreased, the gas temperature at the cold side is further increased, the heat recovery of a solvent system is increased to more than 70 percent from original 50 percent, the thermal energy is further recycled, the energy is saved, the emission is reduced, and the production cost is lowered.
Description
(1) technical field
The present invention relates to a kind of spandex fiber production process heat energy recycle system.Be used for the recycling of spandex fiber production process heat energy.
(2) background technology
In the spandex fiber production process, the mass content that enters polymer (polyurethane) in the spinning solution of filament spinning component is 35%, and all the other 65% are solvent DMAC (N,N-dimethylacetamide).Spinning solution enters the solvent DMAC that needs behind the path in the spinning in the stoste through spinnerets and vapors away fast, remaining polymer cure moulding and through in path, path, false twisting down, oil, operation such as coiling, finally make spandex fibre.
For the solvent DMAC in the stoste that enters spinning shaft is vapored away fast, common production technology is to feed a large amount of about 260 ℃ hot-airs (or nitrogen) in last path, on the one hand the solvent DMAC in the spinning solution is evaporated, take the solvent DMAC that evaporates out of spinning shaft on the other hand.Spinning shaft comes out to contain the hot blast of solvent DMAC through a solvent recovering system, reclaims the solvent DMAC of a part of heat energy and the overwhelming majority.Sending into spinning shaft after gas after solvent recovering system is handled is heated to about 260 ℃ again recycles.
Solvent recovering system is the key equipment in the spandex fiber production process, and its flow chart as shown in Figure 1.Form by one-level heat exchange of heat pipe and level Four condenser and a typhoon machine.Solvent DMAC in the hot blast is that condensation separation is come out by multistage cooling, and concrete technological process is described below:
The hot blast that a plurality of spinning shafts come out to contain solvent DMAC is delivered to solvent recovering system through the airduct of concentrating, and temperature is 200 ℃～210 ℃ when entering the hot side of heat exchange of heat pipe, and the temperature of coming out through heat exchange of heat pipe is 102 ℃; Advance first order surface cooler again, be cooled to 42 ℃ with recirculated cooling water (32 ℃); Advance second level surface cooler again, be cooled to 25 ℃ with chilled water (7 ℃); The supercharging of air intake machine, owing to the effect of mechanical energy, gas temperature can rise to 33 ℃ after the supercharging; Through third level surface cooler, be cooled to 17 ℃ again with chilled water (7 ℃); Through fourth stage surface cooler, be cooled to 2 ℃ again with refrigerant (10 ℃).The DMAC in the gas formed liquid through condensation step by step and discharged from the system bottom this moment, and gas enters the cold side of heat exchange of heat pipe again, and temperature rises to 102 ℃ by 2 ℃.
Existing solvent recovering system adopts the one-level heat exchange of heat pipe, the medium of filling is a demineralized water in the heat pipe, be subjected to the influence of the boiling point (following 100 ℃ of normal pressure) of water to cause the temperature of the hot side gas of heat exchange of heat pipe can't further descend (reaching 98 ℃～102 ℃ at present), the gas temperature of cold side also can't further improve (being no more than 102 ℃) again.
(3) summary of the invention
The objective of the invention is to overcome above-mentioned deficiency, provide a kind of heat exchange more abundant, hot side gas further reduces through the heat exchange temperature, the spandex fiber production process heat energy recycle system that cold side gas further raises through the heat exchange temperature.
The object of the present invention is achieved like this: a kind of spandex fiber production process heat energy recycle system, comprise spinning shaft, first airduct, solvent recovering system, the heating agent heater, second airduct and heating agent or electric heater, described solvent recovering system comprises heat exchange of heat pipe, blower fan and surface cooler, described surface cooler has level Four, be respectively first order surface cooler, second level surface cooler, third level surface cooler and fourth stage surface cooler, described heat exchange of heat pipe has secondary or more than the secondary, the above heat exchange of heat pipe of secondary or secondary is connected in series successively, every grade of interior working media of filling different boiling of heat exchange of heat pipe, and boiling point reduces successively under the working media normal pressure of every grade of interior filling of heat exchange of heat pipe; Described spinning shaft has a plurality of, the hot blast that contains solvent DMAC that a plurality of spinning shafts come out inserts first airduct, the hot blast that first airduct comes out inserts the hot side of chopped-off head heat exchange of heat pipe of solvent recovering system, the gas that the hot side of final stage heat exchange of heat pipe of solvent recovering system is come out inserts first order surface cooler and second level surface cooler successively, the gas that second level surface cooler comes out inserts blower fan, the gas that blower fan comes out inserts third level surface cooler and fourth stage surface cooler successively, the gas that fourth stage surface cooler comes out inserts the final stage heat exchange of heat pipe cold side of solvent recovering system, the gas that the chopped-off head heat exchange of heat pipe cold side of solvent recovering system comes out inserts the heating agent heater, the gas that the heating agent heater comes out inserts second airduct, the gas of second airduct inserts each spinning shaft through the heating agent or the electric heater of each spinning shaft again, so moves in circles.
Spandex fiber production process heat energy recycle of the present invention system, described heat exchange of heat pipe has three grades, be respectively first order heat exchange of heat pipe, second level heat exchange of heat pipe and third level heat exchange of heat pipe, first order heat exchange of heat pipe, second level heat exchange of heat pipe and third level heat exchange of heat pipe are connected in series successively, boiling point is 160 ℃ ± 10 ℃ under the working media normal pressure of filling in the first order heat exchange of heat pipe, boiling point is 100 ℃ ± 5 ℃ under the working media normal pressure of filling in the heat exchange of heat pipe of the second level, boiling point is 80 ℃ ± 5 ℃ under the working media normal pressure of filling in the third level heat exchange of heat pipe, described first airduct inserts the hot side of first order heat exchange of heat pipe of solvent recovering system, and the gas that the hot side of third level heat exchange of heat pipe is come out inserts first order surface cooler.
The hot blast that contains solvent DMAC that a plurality of spinning shafts come out is delivered to solvent recovering system through first airduct, and temperature is 200 ℃-210 ℃ when entering the hot side of first order heat exchange of heat pipe, is 160 ℃ through the come out temperature of described hot blast of first order heat exchange of heat pipe; Through the come out temperature of described hot blast of second level heat exchange of heat pipe is 100 ℃; Through the come out temperature of described hot blast of third level heat exchange of heat pipe is 70 ℃; Advance first order surface cooler again and be cooled to 42 ℃ with 32 ℃ of recirculated cooling waters; Advance second level surface cooler again, be cooled to 25 ℃ with 7 ℃ of chilled waters; The supercharging of air intake machine, gas temperature rise to 33 ℃; Through third level surface cooler, be cooled to 17 ℃ again with 7 ℃ of chilled waters; Again through fourth stage surface cooler, be cooled to 2 ℃ with-10 ℃ of refrigerants, the DMAC in the gas formed liquid through condensation step by step and discharged from the system bottom this moment, and gas enters the cold side of third level heat exchange of heat pipe again, this moment, temperature was 2 ℃, and the temperature of coming out from third level heat exchange of heat pipe is 25 ℃; The temperature of coming out through second level heat exchange of heat pipe is 70 ℃; The temperature of coming out through first order heat exchange of heat pipe is 128 ℃, and the gas temperature that the heating agent heater comes out is 240 ℃, and the gas temperature of second airduct is 230 ℃.
The invention has the beneficial effects as follows:
The present invention changes existing one-level heat exchange of heat pipe into secondary or the above heat exchange of heat pipe of secondary, and substitute original demineralized water with the working media of different boiling, make the temperature further decline (75 ℃) again of the hot side gas of heat exchange of heat pipe, the gas temperature of cold side further improves (128 ℃), the heat recovery of solvent recovering system is brought up to more than 70% by original 50%, further reclaim and utilize heat energy, energy-saving and emission-reduction reduce production costs.
The operation principle of heat pipe is that the liquid medium in the every vacuum tube is vaporized by thermal source (being hot gas herein) heating back, after running into cold medium (herein for cold air) and discharge the latent heat of vaporization to the upper end, be condensed into liquid and fall along tube wall, medium ceaselessly is vaporized in pipe, the circulation of condensation reaches the purpose that heat is transmitted.
When allowing the outlet temperature that is heated side gas reach 128 ℃ and above temperature, this moment heat pipe about 160 ℃ of surface temperature, and adopt water, the about 6.4kg/cm of the saturated vapor pressure when vapor (steam) temperature will reach 160 ℃ as heat transfer medium
2(absolute pressure) that is to say that this moment, every heat pipe need bear 6.4kg/cm
2Pressure.If adopt the liquid medium of boiling point about 160 ℃, the about 1.0kg/cm of the saturated vapor pressure when reaching 160 ℃
2(absolute pressure) reduces heat pipe pressure and improves heat transfer efficiency.
Equally in order to allow the outlet temperature of gas of hot side drop to 75 ℃ and following, the temperature on heat pipe surface is about 50 ℃ at this moment, and employing water is as the words of heat transfer medium, the vapourizing temperature of water under vacuum state is 40 ℃, water in the heat pipe is heated to vaporize to make and loses vacuum in the pipe, water can't further be vaporized, and heat just can't further transmit.If adopt the medium of boiling point about 80 ℃, can guarantee at low temperatures so that medium is vaporized to transmit heat, improve heat transfer efficiency.
(4) description of drawings
Fig. 1 is spandex fiber solvent recovering system schematic flow sheet in the past.
Fig. 2 is a spandex fiber solvent recovering system schematic flow sheet of the present invention.
Reference numeral among the figure:
First order heat exchange of heat pipe 31, second level heat exchange of heat pipe 32, third level heat exchange of heat pipe 33, first order surface cooler 34, second level surface cooler 35, blower fan 36, third level surface cooler 37, fourth stage surface cooler 38, heat exchange of heat pipe 39.
(5) specific embodiment
Referring to Fig. 2, Fig. 2 is a spandex fiber solvent recovering system schematic flow sheet of the present invention.As seen from Figure 2, spandex fiber solvent recovering system of the present invention, comprise spinning shaft 1, first airduct 2, solvent recovering system 3, heating agent heater 4, second airduct 5 and heating agent or electric heater 6, described spinning shaft 1 has a plurality of, the hot blast that contains solvent DMAC that a plurality of spinning shafts 1 come out inserts first airduct 2, first airduct 2 inserts solvent recovering system 3, described solvent recovering system 3 comprises heat exchange of heat pipe, blower fan 36 and surface cooler, described heat exchange of heat pipe comprises secondary or more than the secondary, there are three grades among Fig. 2, be respectively first order heat exchange of heat pipe 31, second level heat exchange of heat pipe 32 and third level heat exchange of heat pipe 33, first order heat exchange of heat pipe 31, fill the working media of different boiling in second level heat exchange of heat pipe 32 and the third level heat exchange of heat pipe 33: boiling point is 160 ℃ ± 10 ℃ under the working media normal pressure of filling in the first order heat exchange of heat pipe 31, mainly contain following working media: N, dinethylformamide (153 ℃), cyclohexanone (155.6 ℃), N,N-dimethylacetamide (166.1 ℃); Boiling point is 100 ℃ ± 5 ℃ under the working media normal pressure of filling in the second level heat exchange of heat pipe 32, mainly adopts demineralized water; Boiling point is 80 ℃ ± 5 ℃ under the working media normal pressure of filling in the third level heat exchange of heat pipe 33, mainly contains following working media: ethanol (78.3 ℃), butanone (79.64 ℃), cyclohexane (80.72 ℃) isopropyl alcohol (82.40 ℃).What the medium selected for use considered that boiling point needs to consider material outward simultaneously is subjected to heat endurance and hypotoxicity, can liquid chemical reaction, different boiling not take place mixes in proportion and reaches corresponding boiling point requirement by multiple simultaneously.First order heat exchange of heat pipe 31, second level heat exchange of heat pipe 32 and third level heat exchange of heat pipe 33 are connected in series successively, and boiling point reduces successively under the working media normal pressure of filling in first order heat exchange of heat pipe 31, second level heat exchange of heat pipe 32 and the third level heat exchange of heat pipe 33.Described first airduct 2 inserts the first order heat exchange of heat pipe 31 hot sides of solvent recovering system 3.Described surface cooler has level Four, be respectively first order surface cooler 34, second level surface cooler 35, third level surface cooler 37 and fourth stage surface cooler 38, the gas that third level heat exchange of heat pipe 33 hot sides are come out inserts first order surface cooler 34 and second level surface cooler 35 successively, the gas that second level surface cooler 35 comes out inserts blower fan 36, the gas that blower fan 36 comes out inserts third level surface cooler 37 and fourth stage surface cooler 38 successively, the gas that fourth stage surface cooler 38 comes out inserts third level heat exchange of heat pipe 33 cold sides, the gas that first order heat exchange of heat pipe 31 cold sides come out inserts heating agent heater 4, the gas that the gas that heating agent heater 4 comes out (240 ℃) inserts second airduct, 5, the second airducts 5 inserts each spinning shaft 1 through the heating agent or the electric heater 6 of each spinning shaft again.
Operation principle:
The hot blast that a plurality of spinning shafts come out contains solvent DMAC is delivered to solvent recovering system through first airduct of concentrating, and temperature is 200 ℃～210 ℃ when entering the hot side of first order heat exchange of heat pipe, is 160 ℃ through the come out temperature of described hot blast of first order heat exchange of heat pipe; Through the come out temperature of described hot blast of second level heat exchange of heat pipe is 100 ℃; Through the come out temperature of described hot blast of third level heat exchange of heat pipe is 70 ℃.Advance first order surface cooler again and be cooled to 42 ℃ with recirculated cooling water (32 ℃); Advance second level surface cooler again, be cooled to 25 ℃ with chilled water (7 ℃); The supercharging of air intake machine, owing to the effect of mechanical energy, gas temperature can rise to 33 ℃ after the supercharging; Through third level surface cooler, be cooled to 17 ℃ again with chilled water (7 ℃); Through fourth stage surface cooler, be cooled to 2 ℃ again with refrigerant (10 ℃).The DMAC in the gas formed liquid through condensation step by step and discharged from the system bottom this moment, and gas enters the cold side of third level heat exchange of heat pipe again, and this moment, temperature was 2 ℃, and the temperature of coming out from third level heat exchange of heat pipe is 25 ℃; The temperature of coming out through second level heat exchange of heat pipe is 70 ℃; The temperature of coming out through first order heat exchange of heat pipe reaches 128 ℃.The gas that first order heat exchange of heat pipe 31 cold sides come out inserts heating agent heater 4, the gas (230 ℃) that the gas that heating agent heater 4 comes out (240 ℃) inserts second airduct, 5, the second airducts 5 inserts each spinning shaft 1 through the heating agent or the electric heater 6 of each spinning shaft again.So move in circles.
Economic measuring and calculating:
Handling air quantity with a cover is 180Nm
3The solvent recovering system of/min is calculated.
Table 1: two kinds of solvent process energy consuming ratios
Adopt the solvent recovering system of the art of this patent can energy-conservation 216kW/h as can be seen from the above table, usually the spandex fiber factory that produces 10000 tons per year needs 12 of such solvent recovering systems, with 8000 hours production times in year, 0.7 yuan/kWh of electricity charge meter, but 1 year energy savings cost approximately: ten thousand yuan of 216*0.7*8000*12=1451.52 have high economic benefit.
Claims (8)
1. spandex fiber production process heat energy recycle system, comprise spinning shaft (1), first airduct (2), solvent recovering system (3), heating agent heater (4), second airduct (5) and heating agent or electric heater (6), described solvent recovering system (3) comprises heat exchange of heat pipe, blower fan (36) and surface cooler, described surface cooler has level Four, be respectively first order surface cooler (34), second level surface cooler (35), third level surface cooler (37) and fourth stage surface cooler (38), it is characterized in that: described heat exchange of heat pipe has secondary or more than the secondary, the above heat exchange of heat pipe of secondary or secondary is connected in series successively, every grade of interior working media of filling different boiling of heat exchange of heat pipe, and boiling point reduces successively under every grade of interior working media normal pressure of filling of heat exchange of heat pipe, described spinning shaft (1) has a plurality of, the hot blast that contains solvent DMAC that a plurality of spinning shafts (1) come out inserts first airduct (2), the hot blast that first airduct (2) comes out inserts the hot side of chopped-off head heat exchange of heat pipe of solvent recovering system (3), the gas that the hot side of final stage heat exchange of heat pipe of solvent recovering system (3) is come out inserts first order surface cooler (34) and second level surface cooler (35) successively, the gas that second level surface cooler (35) comes out inserts blower fan (36), the gas that blower fan (36) comes out inserts third level surface cooler (37) and fourth stage surface cooler (38) successively, the gas that fourth stage surface cooler (38) comes out inserts the final stage heat exchange of heat pipe cold side of solvent recovering system (3), the gas that the chopped-off head heat exchange of heat pipe cold side of solvent recovering system (3) comes out inserts heating agent heater (4), the gas that heating agent heater (4) comes out inserts second airduct (5), the gas of second airduct (5) inserts each spinning shaft (1) through the heating agent or the electric heater (6) of each spinning shaft again, so moves in circles.
2. a kind of spandex fiber production process heat energy recycle according to claim 1 system, it is characterized in that: described heat exchange of heat pipe has three grades, be respectively first order heat exchange of heat pipe (31), second level heat exchange of heat pipe (32) and third level heat exchange of heat pipe (33), first order heat exchange of heat pipe (31), second level heat exchange of heat pipe (32) and third level heat exchange of heat pipe (33) are connected in series successively, boiling point is 160 ℃ ± 10 ℃ under the working media normal pressure of filling in the first order heat exchange of heat pipe (31), boiling point is 100 ℃ ± 5 ℃ under the working media normal pressure of filling in the second level heat exchange of heat pipe (32), boiling point is 80 ℃ ± 5 ℃ under the working media normal pressure of filling in the third level heat exchange of heat pipe (33), described first airduct (2) inserts the hot side of first order heat exchange of heat pipe (31) of solvent recovering system (3), and the gas that the hot side of third level heat exchange of heat pipe (33) is come out inserts first order surface cooler (34).
3. a kind of spandex fiber production process heat energy recycle according to claim 2 system, it is characterized in that: the hot blast that contains solvent DMAC that a plurality of spinning shafts come out is delivered to solvent recovering system through first airduct, temperature is 200 ℃-210 ℃ when entering the hot side of first order heat exchange of heat pipe, is 160 ℃ through the come out temperature of described hot blast of first order heat exchange of heat pipe; Through the come out temperature of described hot blast of second level heat exchange of heat pipe is 100 ℃; Through the come out temperature of described hot blast of third level heat exchange of heat pipe is 70 ℃; Advance first order surface cooler again and be cooled to 42 ℃ with 32 ℃ of recirculated cooling waters; Advance second level surface cooler again, be cooled to 25 ℃ with 7 ℃ of chilled waters; The supercharging of air intake machine, gas temperature rise to 33 ℃; Through third level surface cooler, be cooled to 17 ℃ again with 7 ℃ of chilled waters; Again through fourth stage surface cooler, be cooled to 2 ℃ with-10 ℃ of refrigerants, the DMAC in the gas formed liquid through condensation step by step and discharged from the system bottom this moment, and gas enters the cold side of third level heat exchange of heat pipe again, this moment, temperature was 2 ℃, and the temperature of coming out from third level heat exchange of heat pipe is 25 ℃; The temperature of coming out through second level heat exchange of heat pipe is 70 ℃; The temperature of coming out through first order heat exchange of heat pipe is 128 ℃, and the gas temperature that the heating agent heater comes out is 240 ℃, and the gas temperature of second airduct is 230 ℃.
4. according to claim 2 or 3 described a kind of spandex fiber production process heat energy recycle systems, it is characterized in that: the working media of filling in the described first order heat exchange of heat pipe (31) is N, dinethylformamide, cyclohexanone or N,N-dimethylacetamide.
5. according to claim 2 or 3 described a kind of spandex fiber production process heat energy recycle systems, it is characterized in that: the working media of filling in the described second level heat exchange of heat pipe (32) is a demineralized water.
6. according to claim 2 or 3 described a kind of spandex fiber production process heat energy recycle systems, it is characterized in that: the working media of filling in the described third level heat exchange of heat pipe (33) is ethanol, butanone, cyclohexane or isopropyl alcohol.
7. a kind of spandex fiber production process heat energy recycle according to claim 4 system, it is characterized in that: the working media of filling in the described third level heat exchange of heat pipe (33) is ethanol, butanone, cyclohexane or isopropyl alcohol.
8. a kind of spandex fiber production process heat energy recycle according to claim 4 system, it is characterized in that: the working media of filling in the described third level heat exchange of heat pipe (33) is ethanol, butanone, cyclohexane or isopropyl alcohol; The working media of filling in the described second level heat exchange of heat pipe (32) is a demineralized water.
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Cited By (5)
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| CN102383225A (en) * | 2011-10-25 | 2012-03-21 | 双良节能系统股份有限公司 | Spandex DMAC recovery and heat energy utilization system |
| CN103088447A (en) * | 2013-01-18 | 2013-05-08 | 杭州舒尔姿氨纶有限公司 | Automatic control tunnel balance system applying upper tunnel return air |
| CN103668490A (en) * | 2013-12-23 | 2014-03-26 | 江苏智道工程技术有限公司 | Spandex dry spinning medium circulation method and system |
| CN103849952A (en) * | 2012-11-30 | 2014-06-11 | 杭州益邦氨纶有限公司 | Novel air return system for producing spandex |
| CN111730225A (en) * | 2020-04-24 | 2020-10-02 | 中国化学工程第三建设有限公司 | Large-scale recovery air conditioner assembly installation method |
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| CN111730225A (en) * | 2020-04-24 | 2020-10-02 | 中国化学工程第三建设有限公司 | Large-scale recovery air conditioner assembly installation method |
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|---|---|
| CN101962813B (en) | 2011-09-14 |
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