CN212450664U - New steam condensate water waste heat recovery device - Google Patents
New steam condensate water waste heat recovery device Download PDFInfo
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- CN212450664U CN212450664U CN202021678647.7U CN202021678647U CN212450664U CN 212450664 U CN212450664 U CN 212450664U CN 202021678647 U CN202021678647 U CN 202021678647U CN 212450664 U CN212450664 U CN 212450664U
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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
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- Y02P20/10—Process efficiency
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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
- Y02P20/00—Technologies relating to chemical industry
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- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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Abstract
The utility model provides a new steam condensate water waste heat recovery device mainly relates to steam condensate water waste heat recovery technical field. The new steam condensate water waste heat recovery device comprises a digestion unit, wherein the digestion unit is an alumina low-temperature digestion unit, and the low-temperature digestion unit consists of a sleeve heat exchanger, a heat preservation tank, a flash tank, a dilution tank and a condensate water tank. The beneficial effects of the utility model reside in that: the new steam condensate water of the thermal power plant is recycled twice, the primary ore pulp can be preheated and heated in each cycle, the heat in the primary ore pulp is recovered, the temperature of the condensate water obtained by heat exchange is low, the temperature is generally 80-90 ℃, and the heat of the new steam can be fully utilized; the technical process is simple and easy to operate, does not need to invest new heat exchange equipment, can be well matched and connected with the dissolving-out unit, does not have extra manual maintenance workload, avoids cross-process linkage operation, avoids mutual interference among all processes, and realizes the self thermal cycle utilization of the dissolving-out unit.
Description
Technical Field
The utility model relates to a steam condensate waste heat recovery technical field specifically is a new steam condensate waste heat recovery device.
Background
In the existing Bayer process for producing alumina, the dissolution process is a core link. At present, in a dissolving-out process, a double-pipe heat exchanger is a mainstream heating technology, and flash evaporation exhaust steam preheating and new steam heating technologies are adopted in all alumina plants, so that the new steam consumption is reduced, and the alumina production cost is reduced. In the low-temperature (135-145 ℃) digestion process, the higher the utilization rate of the fresh steam in the heating section is, the lower the temperature of the condensed water after heat exchange is, the lower the digestion steam consumption is, and the lower the production cost of the alumina is. From the current situation of the alumina industry, the utilization rate of new steam is generally low, and the most intuitive performance is that the temperature of condensed water is higher, because the new steam condensed water is returned to a thermal power plant only by recycling once, still contains higher heat, and the heat with available value is not fully utilized.
In order to solve the above problems, the prior art discloses a method for recycling the condensate water of the dissolved new steam, such as the chinese utility model and the utility model patent with publication numbers CN105293544A and CN206069399U, respectively.
The above prior art solutions have the following drawbacks: the utility model CN105293544A sends the dissolved new steam to the evaporation process for reuse, and needs to build a new steam condensate self-evaporator, which has large investment and involves the cross-process operation; utility model patent CN206069399U is for retrieving the comdenstion water waste heat, need pass through plate heat transfer device before sending thermal power plant, and this technique equally needs the fund input, needs artifical the maintenance moreover.
SUMMERY OF THE UTILITY MODEL
In order to solve the defects of the prior art, the utility model provides a new steam condensate waste heat recovery device, the new steam condensate of the thermal power plant of the utility model is recycled twice, the raw ore pulp can be preheated and the temperature can be raised each time, the heat in the raw ore pulp can be recovered, the condensate temperature obtained by the final heat exchange is lower, the general condition is 80-90 ℃, and the new steam heat can be fully utilized; the utility model discloses the simple easy operation of flow need not drop into new indirect heating equipment, can link up with dissolving out the good supporting of unit, does not have extra manual maintenance work load, has avoided striding the process linkage operation simultaneously, has stopped the interference of each other between each process, has realized the thermal cycle who dissolves out unit self and has utilized.
The utility model discloses a realize above-mentioned purpose, realize through following technical scheme:
a new steam condensate waste heat recovery device comprises a stripping unit, wherein the stripping unit is an alumina low-temperature stripping unit, the low-temperature stripping unit is composed of a sleeve heat exchanger, a heat preservation tank, a flash tank, a dilution rear tank and a condensate water tank, the stripping unit is heated by an eight-stage sleeve heat exchanger, the first to fifth stages are preheating stages, the sixth to eighth stages are heating stages, the first stage sleeve heat exchanger is preheated by new steam condensate preheated by the fifth stage sleeve heat exchanger, the second to fourth stage sleeve heat exchangers are preheated by flash evaporation exhaust steam, the fifth stage sleeve heat exchanger is preheated by new steam condensate of the sixth to eighth stage sleeve heat exchangers, the sixth to eighth stage sleeve heat exchangers are heated by new steam of a thermal power plant, each stage of the stripping unit sleeve heat exchanger is provided with a corresponding condensate water tank for receiving condensate water after heat exchange, the first-stage condensed water tank is connected with an outward-feeding pump and is conveyed to a thermal power plant by a pump, the water outlet of the second-fourth-stage condensed water tank is collected into a header pipe, the header pipe is connected with the outward-feeding pump and is conveyed to a red mud washing procedure by the pump, and the water outlet of the sixth-eighth-stage condensed water tank is collected into a header pipe and then is preheated by a fifth-stage double-pipe heat exchanger.
Furthermore, the digestion unit adopts a Bayer process low-temperature digestion production process, and the digestion temperature is 135-145 ℃.
Further, the dissolving-out unit preheats the raw ore pulp by a sleeve heat exchanger, the raw ore pulp is heated to the dissolving-out temperature of 135-145 ℃, then the dissolving-out reaction is carried out in a heat preservation tank, the dissolved-out ore pulp after the reaction is cooled and depressurized by a three-stage flash tank, then the discharged material enters a diluting tank, and flash evaporation exhaust steam is used for preheating the raw ore pulp.
Furthermore, the preheating section of the sleeve of the digestion unit is preheated by adopting flash evaporation exhaust steam and new steam condensate water medium, the flash evaporation exhaust steam is obtained by flash evaporation of the digestion ore pulp, and the new steam condensate water is obtained by condensing the new steam heating raw ore pulp.
Furthermore, the heating section of the sleeve of the dissolution unit is heated by a new steam medium supplied by a thermal power plant, the new steam pressure is 0.7-0.9 Mpa, and the temperature is 210-220 ℃.
Furthermore, the heating medium of the double-pipe heat exchanger enters a corresponding condensate water tank for collection after heat exchange, flash evaporation exhaust steam condensate water is collected and then sent to a settling process to be used as red mud washing water, and new steam condensate water is collected and then sent to a thermal power plant for reuse.
Contrast prior art, the beneficial effects of the utility model are that:
the utility model discloses the new steam condensate water cyclic utilization of hot power plant is twice, and each circulation can preheat the raw ore pulp and carry out the temperature raising, retrieves the heat in it, and the condensate water temperature that the last heat transfer obtained is lower, and general condition is at 80 ~ 90 ℃, and new steam heat can make full use of; the utility model discloses the simple easy operation of flow need not drop into new indirect heating equipment, can link up with dissolving out the good supporting of unit, does not have extra manual maintenance work load, has avoided striding the process linkage operation simultaneously, has stopped the interference of each other between each process, has realized the thermal cycle who dissolves out unit self and has utilized.
Drawings
FIG. 1 is a schematic structural view of the present invention;
Detailed Description
The present invention will be further described with reference to the accompanying drawings and specific embodiments. It should be understood that these examples are for illustrative purposes only and are not intended to limit the scope of the present invention. Furthermore, it should be understood that various changes or modifications of the present invention may be made by those skilled in the art after reading the teachings of the present invention, and these equivalents also fall within the scope defined in the present application.
As shown in fig. 1, the utility model relates to a new steam condensate water waste heat recovery device, which comprises a dissolving-out unit, wherein the dissolving-out unit is an alumina low-temperature dissolving-out unit, the low-temperature dissolving-out unit is composed of a sleeve pipe heat exchanger, a heat preservation tank, a flash evaporation tank, a dilution back tank and a condensation water tank, the dissolving-out unit is heated by eight-stage sleeve pipe heat exchangers, wherein the first to fifth stages are preheating stages, the sixth to eighth stages are heating stages, the first stage sleeve pipe heat exchanger adopts new steam condensate water preheated by the fifth stage sleeve pipe heat exchanger, the second to fourth stage sleeve pipe heat exchangers adopt flash evaporation exhaust steam for preheating, the fifth stage sleeve pipe heat exchanger adopts new steam condensate water by the sixth to eighth stage sleeve pipe heat exchangers, the sixth to eighth stage sleeve pipe heat exchangers adopt new steam of a thermal power plant for heating, each stage of the dissolving-out unit sleeve pipe heat exchanger is provided with a corresponding condensation, the first-stage condensed water tank is connected with an external pump and is pumped to a thermal power plant, the water outlet of the second-fourth-stage condensed water tank is collected into a header pipe, the header pipe is connected with the external pump and is pumped to the red mud washing procedure, the water outlet of the sixth-eighth-stage condensed water tank is collected into a header pipe, and then the header pipe is preheated by a fifth-stage double-pipe heat exchanger.
Specifically, the digestion unit adopts a Bayer process low-temperature digestion production process, and the digestion temperature is 135-145 ℃.
Specifically, the dissolving-out unit preheats raw ore pulp by a sleeve heat exchanger, the raw ore pulp is heated to the dissolving-out temperature of 135-145 ℃, then the dissolving-out reaction is carried out in a heat preservation tank, the dissolved-out ore pulp after the reaction is cooled and depressurized by a three-stage flash tank, then the discharged material enters a diluting tank, and flash evaporation exhaust steam is used for preheating the raw ore pulp.
Specifically, the preheating section of the sleeve of the digestion unit is preheated by adopting flash evaporation exhaust steam and new steam condensate water medium, the flash evaporation exhaust steam is obtained by flash evaporation of digestion ore pulp, and the new steam condensate water is obtained by condensing new steam heated raw ore pulp.
Specifically, the heating section of the sleeve of the dissolution unit is heated by a new steam medium supplied by a thermal power plant, the new steam pressure is 0.7-0.9 Mpa, and the temperature is 210-220 ℃.
Specifically, the heating medium of the double-pipe heat exchanger enters a corresponding condensate water tank for collection after heat exchange, flash evaporation exhaust steam condensate water is collected and then sent to a settling process to be used as red mud washing water, and new steam condensate water is collected and then sent to a thermal power plant for reuse.
Example (b):
when using this device, at first add the primary pulp to first order double-pipe heat exchanger in from the primary pulp import, the primary pulp is through the heat transfer after the heat transfer ejection of compact get into second level double-pipe heat exchanger that raises the temperature, through ejection of compact to the holding vessel after eighth level double-pipe heat exchanger raises the temperature in proper order, and the primary pulp dissolves out the reaction in the holding vessel, dissolves out the pulp and enters the flash tank cooling decompression after the reaction finishes, discharges to the back groove of diluting after tertiary flash distillation again.
The utility model discloses the new steam condensate water cyclic utilization of hot power plant is twice, and each circulation can preheat the raw ore pulp and carry out the temperature raising, retrieves the heat in it, and the condensate water temperature that the last heat transfer obtained is lower, and general condition is at 80 ~ 90 ℃, and new steam heat can make full use of; the utility model discloses the simple easy operation of flow need not drop into new indirect heating equipment, can link up with dissolving out the good supporting of unit, does not have extra manual maintenance work load, has avoided striding the process linkage operation simultaneously, has stopped the interference of each other between each process, has realized the thermal cycle who dissolves out unit self and has utilized.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit it; although the present invention has been described in detail with reference to the foregoing embodiments, it should be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; such modifications and substitutions do not depart from the spirit and scope of the present invention.
Claims (6)
1. The utility model provides a new steam condensate water waste heat recovery device, includes dissolves out the unit, its characterized in that: the digestion unit is an alumina low-temperature digestion unit, the low-temperature digestion unit consists of a sleeve heat exchanger, a heat preservation tank, a flash tank, a diluting rear tank and a condensed water tank, the digestion unit is heated by an eight-stage sleeve heat exchanger, wherein the first to the fifth stages are preheating stages, the sixth to the eighth stages are heating stages, the first stage sleeve heat exchanger is preheated by new steam condensed water preheated by the fifth stage sleeve heat exchanger, the second to the fourth stage sleeve heat exchangers are preheated by flash exhausted steam, the fifth stage sleeve heat exchanger is preheated by new steam condensed water of the sixth to the eighth stage sleeve heat exchangers, the sixth to the eighth stage sleeve heat exchangers are heated by new steam of a thermal power plant, each stage of the sleeve heat exchanger of the digestion unit is provided with a corresponding condensed water tank for receiving the condensed water after heat exchange, and the first stage condensed water tank is connected with an outward-feeding pump, and the water from the sixth-eighth stage condensed water tanks is collected into a header pipe and then sent to a fifth-stage double-pipe heat exchanger for preheating.
2. The fresh steam condensate waste heat recovery device of claim 1, wherein: the digestion unit adopts a Bayer process low-temperature digestion production process, and the digestion temperature is 135-145 ℃.
3. The fresh steam condensate waste heat recovery device of claim 1, wherein: the dissolving-out unit preheats the raw ore pulp by adopting a sleeve heat exchanger, the raw ore pulp is heated to reach the dissolving-out temperature of 135-145 ℃, then the dissolving-out reaction is carried out in a heat preservation tank, the dissolved-out ore pulp after the reaction is cooled and depressurized by a three-stage flash tank, then the discharged material enters a diluting rear tank, and flash evaporation exhaust steam is used for preheating the raw ore pulp.
4. The fresh steam condensate waste heat recovery device of claim 1, wherein: the preheating section of the digestion unit sleeve is preheated by adopting flash evaporation exhaust steam and a new steam condensate water medium, the flash evaporation exhaust steam is obtained by flash evaporation of digestion ore pulp, and the new steam condensate water is obtained by condensing the new steam heated original ore pulp.
5. The fresh steam condensate waste heat recovery device of claim 1, wherein: the heating section of the dissolving-out unit sleeve is heated by a new steam medium supplied by a thermal power plant, the new steam pressure is 0.7-0.9 Mpa, and the temperature is 210-220 ℃.
6. The fresh steam condensate waste heat recovery device of claim 1, wherein: the heating medium of the double-pipe heat exchanger enters a corresponding condensate water tank for collection after heat exchange, flash evaporation exhaust steam condensate water is collected and then sent to a sedimentation process to be used as red mud washing water, and new steam condensate water is collected and then sent to a thermal power plant for reuse.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202021678647.7U CN212450664U (en) | 2020-08-13 | 2020-08-13 | New steam condensate water waste heat recovery device |
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| CN202021678647.7U CN212450664U (en) | 2020-08-13 | 2020-08-13 | New steam condensate water waste heat recovery device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112125324A (en) * | 2020-08-13 | 2020-12-25 | 山东南山铝业股份有限公司 | New steam condensate water waste heat recovery device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112125324A (en) * | 2020-08-13 | 2020-12-25 | 山东南山铝业股份有限公司 | New steam condensate water waste heat recovery device |
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