CN205227896U - Condensate water is recovery system again - Google Patents
Condensate water is recovery system again Download PDFInfo
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- CN205227896U CN205227896U CN201520828177.0U CN201520828177U CN205227896U CN 205227896 U CN205227896 U CN 205227896U CN 201520828177 U CN201520828177 U CN 201520828177U CN 205227896 U CN205227896 U CN 205227896U
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Abstract
The utility model provides a condensate water is recovery system again which the structure is connected to entry on the heat exchanger for stone brain oil pipe says, export that heat exchanger and this entry correspond through first pipe connection to deoxidizing the tata top, pass through another entry of second pipe connection to heat exchanger at the bottom of the deoxidation tata, the air cooler is expected with another export that corresponds that enters the mouth through third pipe connection to the bottoms that deoxidizes to the heat exchanger, two dodge jar through fourth pipe connection to the water pitcher that condenses, the 5th pipe connection of rethread to condensate pump, the condensate water is connected to enthalpy exchanger tube side entry in advance by the power plant through tube side inlet pipe, in advance the export of enthalpy exchanger tube side be connected to the condensate water return wire through tube side export pipeline, retrieve the low temperature condensate water through the condensate water return wire. The utility model discloses retrieve 0.46Mpa steam waste heat, thereby set up in advance the increase that enthalpy exchanger has increased original heat exchanger tube side exit temperature and shell side exit temperature, tube side exit temperature for the deoxidation top temperature increases, shell side exit temperature's rising.
Description
Technical field
The utility model belongs to field of chemical equipment, is specifically related to a kind of condensate water recovery system again.
Background technology
Low pressure, middle pressure steam is utilized to carry out thermal source in a lot of chemical industry at present, the condensate water produced produces 1.0mpa and 0.46Mpa steam by flash distillation, remaining condensing water temperature large about 100 DEG C, this part condensate water general is not effectively utilized, simultaneously 0.46Mpa steam with waste heat be not also utilized, thus cause huge energy waste.
Summary of the invention
In view of prior art Problems existing, the utility model provides a kind of condensate water recovery system again, recyclable low-temperature condensate, and reclaims 0.46Mpa steam.
For achieving the above object, the technical scheme that the utility model adopts is a kind of condensate water recovery system again, and it comprises naphtha pipeline, heat exchanger, the first pipeline, deoxidation tower, second pipe, the 3rd pipeline, deoxidation materials at bottom of tower air cooler, two dodges tank, the 4th pipeline, condense water pot, the 5th pipeline, condensate pump, power plant condensation waterpipe, tube-side inlet pipeline, preheating heat exchanger, tube side outlet conduit, shell side inlet pipeline, shell-side outlet pipeline, the condensate water line of return, described naphtha pipeline is connected to heat exchanger entrance, the outlet that heat exchanger is corresponding with this entrance is connected to deoxidation tower tower top by the first pipeline, be connected to another entrance of heat exchanger by second pipe at the bottom of deoxidation tower tower, the outlet that heat exchanger is corresponding with another entrance is connected to deoxidation materials at bottom of tower air cooler by the 3rd pipeline, described two dodge tank is connected to condensation water pot by the 4th pipeline, condensation water pot is connected to condensate pump by the 5th pipeline, condensate pump connects power plant condensation waterpipe, power plant condensation waterpipe is connected to preheating heat exchanger tube-side inlet by tube-side inlet pipeline, the outlet of preheating heat exchanger tube side is connected to the condensate water line of return by tube side outlet conduit, the condensate water line of return is connected to the 4th pipeline, naphtha pipeline is connected to preheating heat exchanger shell side inlet by shell side inlet pipeline, preheating heat exchanger shell-side outlet is connected to naphtha pipeline one end near heat exchanger by shell-side outlet pipeline.The described condensate water line of return comprises the 6th pipeline, air and liquid mixer, the 7th pipeline, 0.46Mpa jet chimney; Tube side outlet conduit is connected to air and liquid mixer by the 6th pipeline, and air and liquid mixer is connected to the 4th pipeline by the 7th pipeline, and 0.46Mpa jet chimney is connected to air and liquid mixer.Described air and liquid mixer inlet temperature is 70 DEG C, and air and liquid mixer outlet temperature is 110 DEG C.Described tube side outlet conduit is connected to power plant condensation waterpipe by the 8th pipeline.The described condensate water line of return is connected to power plant condensation waterpipe by the 9th pipeline.Described preheating heat exchanger shell side inlet temperature is 0 DEG C, and preheating heat exchanger shell-side outlet temperature is 40 DEG C; Preheating heat exchanger tube-side inlet temperature is 110 DEG C, and preheating heat exchanger tube side outlet temperature is 70 DEG C.Described naphtha pipeline pipeline pressure is 0.8Mpa, and flow is 300t/h.Described condensate pump outlet pressure is 0.8Mpa.Described preheating heat exchanger heat exchange area is 200m
2.Described shell side inlet pipeline is DN350 steel pipe, and tube-side inlet pipeline is DN200 steel pipe.
Brief description of the process: the condensate water sent by Technical Revamping Design condensate pump of this Aromatic Hydrocarbon United Plant is heated the naphtha from tank field, and the naphtha after heating makes it to enter original deoxidation tower after temperature reaches 110 DEG C by original heat exchanger again.Condensate water causes newly-increased naphtha preheating heat exchanger from 1 district piping lane condensate water house steward, condensate water part after heat exchange enters in air and liquid mixer, (air and liquid mixer is exactly that side passes into condensate water, passes into 0.46Mpa steam at top to absorb unnecessary 0.46Mpa steam, both mixing are by circulating water heating low for temperature, 0.46Mpa steam is reduced temperature, be transformed into condensate water), condensed water absorption steam enters original condensation water pot after heating up in the lump, and remaining condensate water sends power plant outside.
Condensate water dodges tank from two, be sent to condensation water pot, condensing water temperature is about 110 DEG C, pass through condensate pump, condensate pump outlet pressure is 0.8Mpa, make condensate water first through preheating heat exchanger, naphtha be carried out in tank field to heat, after heat exchange, temperature is that the cryogenic condensation water of 70 DEG C is sent to power plant by power plant condensation waterpipe, the condensate water line of return is set up for maintaining condensation water pot liquid level, by the condensate water after line of return heat exchange through air and liquid mixer, 0.46Mpa steam is passed into condensate water by air and liquid mixer, condensation water pot is entered to after condensed water being heated to 110 DEG C, recycle.
The beneficial effects of the utility model: reclaim low-temperature condensate, and reclaim 0.46Mpa steam waste heat, economize energy more, greatly reduces production cost.Reduce the steam use amount of deoxidation tower reboiler specifically, set up preheating heat exchanger thus add original heat exchanger tube pass outlet temperature, and shell-side outlet temperature, the increase of tube side outlet temperature, deoxidation tower top temperature is increased, and the rising of shell-side outlet temperature, is beneficial to reaction more.
Other illustrate:
1, the pressure in preheating heat exchanger oil circuit and water route, must guarantee that water route pressure is greater than oil circuit pressure, if heat exchanger tube can ensure that water is altered in oil after there is leakage, is evaporated by water by deoxidation tower.
2, the condensing capacity owing to being sent to power plant summer is less, and preheating heat exchanger uses condensate water less, therefore the condensate water line of return does not come into operation, and to the condensate water line of return that comes into operation during winter, reclaims 0.46Mpa steam, avoids 0.46Mpa steam evacuation.
3, a condensed water consumption part sends to power plant by power plant condensation waterpipe, and a part returns condensate water pot through the condensate water line of return.
Accompanying drawing explanation
Fig. 1 is process chart of the present utility model;
Fig. 2 is steam use amount Long-term change trend figure;
Fig. 3 is the changing trend diagram of naphtha feed amount;
Fig. 4 is deoxidation tower tower top temperature changing trend diagram;
Fig. 5 is the changing trend diagram of deoxidation tower column bottom temperature;
Fig. 6 is deoxidation materials at bottom of tower air cooler gateway temperature comparisons's tendency chart;
In figure: 1, naphtha pipeline, 2, heat exchanger, 3, first pipeline, 4, deoxidation tower, 5, second pipe, 6, 3rd pipeline, 7, deoxidation materials at bottom of tower air cooler, 8, two dodge tank, 9, 4th pipeline, 10, condensation water pot, 11, 5th pipeline, 12, condensate pump, 13, power plant condensation waterpipe, 14, tube-side inlet pipeline, 15, preheating heat exchanger, 16, tube side outlet conduit, 17, shell side inlet pipeline, 18, shell-side outlet pipeline, 19, 6th pipeline, 20, air and liquid mixer, 21, 7th pipeline, 22, 0.46Mpa jet chimney, 23, 8th pipeline, 24, 9th pipeline.
Detailed description of the invention
A kind of condensate water recovery system again, it comprises naphtha pipeline 1, heat exchanger 2, first pipeline 3, deoxidation tower 4, second pipe 5, the 3rd pipeline 6, deoxidation materials at bottom of tower air cooler 7, two dodges tank 8, the 4th pipeline 9, condense water pot 10, the 5th pipeline 11, condensate pump 12, power plant condensation waterpipe 13, tube-side inlet pipeline 14, preheating heat exchanger 15, tube side outlet conduit 16, shell side inlet pipeline 17, shell-side outlet pipeline 18, the condensate water line of return, described naphtha pipeline 1 is connected to heat exchanger 2 one entrances, the outlet that heat exchanger 2 is corresponding with this entrance is connected to deoxidation tower 4 tower top by the first pipeline 3, be connected to another entrance of heat exchanger 2 by second pipe 5 at the bottom of deoxidation tower 4 tower, the outlet that heat exchanger 2 is corresponding with another entrance is connected to deoxidation materials at bottom of tower air cooler 7 by the 3rd pipeline 6, described two dodge tank 8 is connected to condensation water pot 10 by the 4th pipeline 9, condensation water pot 10 is connected to condensate pump 12 by the 5th pipeline 11, condensate pump 12 connects power plant condensation waterpipe 13, power plant condensation waterpipe 13 is connected to preheating heat exchanger 15 tube-side inlet by tube-side inlet pipeline 14, the outlet of preheating heat exchanger 15 tube side is connected to the condensate water line of return by tube side outlet conduit 16, the condensate water line of return is connected to the 4th pipeline 9, naphtha pipeline 1 is connected to preheating heat exchanger 15 shell side inlet by shell side inlet pipeline 17, preheating heat exchanger 15 shell-side outlet is connected to naphtha pipeline 1 one end near heat exchanger 2 by shell-side outlet pipeline 16.The described condensate water line of return comprises the 6th pipeline 19, air and liquid mixer 20, the 7th pipeline 21,0.46Mpa jet chimney 22; Tube side outlet conduit 16 is connected to air and liquid mixer 20 by the 6th pipeline, and air and liquid mixer (20) is connected to the 4th pipeline 9,0.46Mpa jet chimney 22 by the 7th pipeline 21 and is connected to air and liquid mixer 20.Described air and liquid mixer 20 inlet temperature is 70 DEG C, and air and liquid mixer 20 outlet temperature is 110 DEG C.Described tube side outlet conduit 16 is connected to power plant condensation waterpipe 13 by the 8th pipeline 23.The described condensate water line of return is connected to power plant condensation waterpipe 13 by the 9th pipeline 24.Described preheating heat exchanger 15 shell side inlet temperature is 0 DEG C, and preheating heat exchanger 15 shell-side outlet temperature is 40 DEG C; Preheating heat exchanger (15) tube-side inlet temperature is 110 DEG C, and preheating heat exchanger 15 tube side outlet temperature is 70 DEG C.Described naphtha pipeline 1 pipeline pressure is 0.8Mpa, and flow is 300t/h.Described condensate pump 12 outlet pressure is 0.8Mpa.Described preheating heat exchanger 15 heat exchange area is 200m
2.Described shell side inlet pipeline 17 is DN350 steel pipe, and tube-side inlet pipeline 14 is DN200 steel pipe.
Brief description of the process: the condensate water sent by Technical Revamping Design condensate pump of this Aromatic Hydrocarbon United Plant is heated the naphtha from tank field, and the naphtha after heating makes it to enter original deoxidation tower after temperature reaches 110 DEG C by original heat exchanger again.Condensate water causes newly-increased naphtha preheating heat exchanger from condensate water house steward, condensate water part after heat exchange enters in air and liquid mixer, absorb unnecessary 0.46Mpa steam, condensed water absorption steam enters original condensation water pot after heating up in the lump, and remaining condensate water sends power plant outside.
Condensate water dodges tank from two, be sent to condensation water pot, condensing water temperature is about 110 DEG C, pass through condensate pump, condensate pump outlet pressure is 0.8Mpa, make condensate water first through preheating heat exchanger, naphtha be carried out in tank field to heat, after heat exchange, temperature is that the cryogenic condensation water of 70 DEG C is sent to power plant by power plant condensation waterpipe, the condensate water line of return is set up for maintaining condensation water pot liquid level, by the condensate water after line of return heat exchange through air and liquid mixer, 0.46Mpa steam is passed into condensate water by air and liquid mixer, condensation water pot is entered to after condensed water being heated to 110 DEG C, recycle.
Date comprision after coming into operation:
Data record after heat exchanger comes into operation:
(1) come into operation record sheet:
(2) data analysis:
(2.1) steam use amount Long-term change trend figure is as shown in Figure 2,
As seen from Figure 2, after preheating heat exchanger comes into operation, deoxidation tower tower reboiler steam use amount reduces more, on average reduces about 3.5t/h steam, and steam use amount is low is in earlier stage because feed loading is lower.
(2.2) changing trend diagram of naphtha feed amount is as shown in Figure 3,
Found out by Fig. 3, along with pre-hydrogenation maintenance is complete, pre-hydrogenation inlet amount increases gradually, comparatively upper figure contrasts, deoxidation tower tower reboiler steam consumption maintains 7.3t/h substantially, usually analyze, increasing along with the increase of inlet amount of the steam use amount of deoxidation tower tower reboiler, therefore can find out preheating heat exchanger come into operation after effect.
(2.3) deoxidation tower tower top temperature changing trend diagram is as shown in Figure 4,
After preheating heat exchanger comes into operation, by lower steam use amount, tower top temperature is higher, part light component is made to enter in return tank by air cooling, according to former ruuning situation, want to improve this tower top temperature, the steam use amount of tower bottom reboiler must be strengthened.
(2.4) changing trend diagram of deoxidation tower column bottom temperature is as shown in Figure 5,
Found out by Fig. 5, reduce deoxidation tower tower reboiler steam amount after preheating heat exchanger comes into operation, column bottom temperature is basically identical, and because the change of processing oil product weight ratio strengthens in the recent period, during processing light oil, column bottom temperature is lower, and during heavy oil with before, temperature is consistent.
(2.5) deoxidation materials at bottom of tower air cooler gateway temperature comparisons's tendency chart is as shown in Figure 6, and A-106 is deoxidation materials at bottom of tower air cooler:
After finding out that preheating heat exchanger comes into operation by Fig. 6, add heat exchanger tube pass outlet temperature, and shell-side outlet temperature, the increase of tube side outlet temperature, deoxidation tower tower top temperature is increased, the rising of shell-side outlet temperature, add deoxidation materials at bottom of tower air cooler air cooling load, increase the operation of two air cooling blower fans, control cold rear temperature ≯ 60 DEG C.
Preheating heat exchanger comes into operation energy-saving analysis:
1, as can be seen from the above table, this is calculated as 4-10 in summer month cost saving, the 1.0Mpa steam saving 3.5 tons per hour, through docking with operating company, current 1.0Mpa steam price is 197 yuan/ton, the electricity charge, by 0.6 yuan/degree, calculate, and cost saving is for saving steam expense-consumption electricity charge=3475080-133056=3342024 unit altogether
1., equipment and materials expense 2, through dock with equipment, instrument, this time preheating heat exchanger improvement expenses comprises:, 184282.92 yuan altogether; 2., instrument material expense, amount to 47537.73 yuan; 3., operating expenses, amount to 100000 yuan; 4., design cost, amount to 50000 yuan, amount to investment cost be:
184282.92+47537.73+100000+50000=381820.65 first
The utility model reclaims low-temperature condensate, and reclaims 0.46Mpa steam waste heat, and economize energy more, greatly reduces production cost.Reduce the steam use amount of deoxidation tower reboiler specifically, set up preheating heat exchanger thus add original heat exchanger tube pass outlet temperature, and shell-side outlet temperature, the increase of tube side outlet temperature, deoxidation tower top temperature is increased, and the rising of shell-side outlet temperature, is beneficial to reaction more.
Claims (4)
1. condensate water recovery system again, it is characterized in that: comprise naphtha pipeline (1), heat exchanger (2), first pipeline (3), deoxidation tower (4), second pipe (5), 3rd pipeline (6), deoxidation materials at bottom of tower air cooler (7), two dodge tank (8), 4th pipeline (9), condensation water pot (10), 5th pipeline (11), condensate pump (12), power plant condensation waterpipe (13), tube-side inlet pipeline (14), preheating heat exchanger (15), tube side outlet conduit (16), shell side inlet pipeline (17), shell-side outlet pipeline (18), the condensate water line of return, described naphtha pipeline (1) is connected to heat exchanger (2) entrances, the outlet that heat exchanger (2) is corresponding with this entrance is connected to deoxidation tower (4) tower top by the first pipeline (3), be connected to heat exchanger (2) another entrance by second pipe (5) at the bottom of deoxidation tower (4) tower, the outlet that heat exchanger (2) is corresponding with another entrance is connected to deoxidation materials at bottom of tower air cooler (7) by the 3rd pipeline (6), described two dodge tank (8) is connected to condensation water pot (10) by the 4th pipeline (9), condensation water pot (10) is connected to condensate pump (12) by the 5th pipeline (11), condensate pump (12) connects power plant condensation waterpipe (13), power plant condensation waterpipe (13) is connected to preheating heat exchanger (15) tube-side inlet by tube-side inlet pipeline (14), the outlet of preheating heat exchanger (15) tube side is connected to the condensate water line of return by tube side outlet conduit (16), the condensate water line of return is connected to the 4th pipeline (9), naphtha pipeline (1) is connected to preheating heat exchanger (15) shell side inlet by shell side inlet pipeline (17), preheating heat exchanger (15) shell-side outlet is connected to naphtha pipeline (1) one end near heat exchanger (2) by shell-side outlet pipeline (16).
2. a kind of condensate water according to claim 1 recovery system again, is characterized in that: described tube side outlet conduit (16) is connected to power plant condensation waterpipe (13) by the 8th pipeline (23).
3. a kind of condensate water according to claim 1 recovery system again, is characterized in that: the described condensate water line of return is connected to power plant condensation waterpipe (13) by the 9th pipeline (24).
4. a kind of condensate water according to claim 1 recovery system again, is characterized in that: described preheating heat exchanger (15) heat exchange area is 200m
2.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520828177.0U CN205227896U (en) | 2015-10-26 | 2015-10-26 | Condensate water is recovery system again |
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| CN201520828177.0U CN205227896U (en) | 2015-10-26 | 2015-10-26 | Condensate water is recovery system again |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105371512A (en) * | 2015-10-26 | 2016-03-02 | 大连福佳·大化石油化工有限公司 | Condensation water recycling system |
| CN111167144A (en) * | 2020-02-27 | 2020-05-19 | 中国华能集团清洁能源技术研究院有限公司 | Sectional condensation type desulfurization slurry flash evaporation heat extraction water taking device and method |
-
2015
- 2015-10-26 CN CN201520828177.0U patent/CN205227896U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105371512A (en) * | 2015-10-26 | 2016-03-02 | 大连福佳·大化石油化工有限公司 | Condensation water recycling system |
| CN111167144A (en) * | 2020-02-27 | 2020-05-19 | 中国华能集团清洁能源技术研究院有限公司 | Sectional condensation type desulfurization slurry flash evaporation heat extraction water taking device and method |
| CN111167144B (en) * | 2020-02-27 | 2023-08-08 | 中国华能集团清洁能源技术研究院有限公司 | Device and method for flash evaporation extraction of hot water from desulfurization slurry by zone condensation |
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