CN220206416U - ORC cascade utilization's esterification steam condensate water waste heat recovery device - Google Patents
ORC cascade utilization's esterification steam condensate water waste heat recovery device Download PDFInfo
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- CN220206416U CN220206416U CN202323062167.4U CN202323062167U CN220206416U CN 220206416 U CN220206416 U CN 220206416U CN 202323062167 U CN202323062167 U CN 202323062167U CN 220206416 U CN220206416 U CN 220206416U
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 62
- 238000011084 recovery Methods 0.000 title claims abstract description 31
- 239000002918 waste heat Substances 0.000 title claims abstract description 31
- 230000032050 esterification Effects 0.000 title claims abstract description 24
- 238000005886 esterification reaction Methods 0.000 title claims abstract description 24
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims abstract description 36
- 238000000926 separation method Methods 0.000 claims abstract description 16
- 238000010248 power generation Methods 0.000 claims abstract description 8
- 239000007789 gas Substances 0.000 claims description 40
- 238000010992 reflux Methods 0.000 claims description 29
- 239000007788 liquid Substances 0.000 claims description 25
- 238000001816 cooling Methods 0.000 claims description 16
- 239000000498 cooling water Substances 0.000 claims description 11
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 claims description 9
- 238000011143 downstream manufacturing Methods 0.000 claims description 6
- 230000005484 gravity Effects 0.000 claims description 6
- 230000001105 regulatory effect Effects 0.000 claims description 4
- 238000000034 method Methods 0.000 claims description 2
- 238000004064 recycling Methods 0.000 claims 2
- 239000002699 waste material Substances 0.000 abstract description 4
- 229920000728 polyester Polymers 0.000 abstract description 3
- 238000010586 diagram Methods 0.000 description 4
- 230000005540 biological transmission Effects 0.000 description 2
- 238000011045 prefiltration Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000000844 transformation Methods 0.000 description 1
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model discloses an ORC cascade utilization esterification steam condensate water waste heat recovery device, which comprises an evaporator and an ethylene glycol separation tower; the device also comprises a steam preheater, a condensate tank and a heat regenerator; the evaporator is connected with the steam preheater through a first pipeline and a second pipeline, and the evaporator is connected with the condensate tank through a third pipeline; the steam preheater is connected with the condensate tank through a fourth pipeline and a fifth pipeline, the steam preheater is connected with the condensate preheater through a sixth pipeline, and the condensate preheater is connected with the condensate tank through a seventh pipeline; compared with the prior art, the heat contained in the esterification steam is utilized in a cascade way as much as possible, and the recovery efficiency of steam condensate water is improved; the waste of steam condensate heat is reduced, the efficiency of the ORC waste heat power generation system is improved, and the operation cost, the labor cost, the transportation cost and the like of a polyester workshop are reduced.
Description
Technical Field
The utility model relates to the field of ORC power generation equipment, in particular to an esterification steam condensate water waste heat recovery device for ORC cascade utilization.
Background
In the polyester chemical industry, the esterified steam with more than 100 degrees from the top of the glycol separation tower is generally cooled and condensed directly, and condensed water is returned to a reflux tank, so that the higher heat energy of the esterified steam and the condensed steam is directly wasted, and energy waste is caused if the condensed steam in a pipeline is directly discharged. The esterified steam from the top of the glycol separation tower is cooled and condensed, a special cooling system is required to be designed, the power consumption of the cooling tower and the water pump and the circulating use amount of cooling water are increased, and the production cost of enterprises is increased to a certain extent.
At present, the domestic steam condensate recovery system generally adopts an open type collection and long-distance pipeline self-flow transmission or pressure transmission recovery mode. However, after long-time use, the automatic control degree of the steam condensate recovery system is lower, the temperature of the recovered condensate is not stable and adjustable, and the recovery rate of the steam condensate is low.
On one hand, the existing ORC waste heat recovery system design does not recycle the waste heat of steam condensate water and collect and discharge non-condensable gas as a part of the system design; on the other hand, the waste heat of saturated esterified vapor having a constant temperature and positive pressure is not sufficiently utilized in steps. In the existing design, most of the esterified steam with certain temperature and pressure is changed into steam condensate water through a traditional water-cooling or air-cooling device, and finally the condensate water is returned to a reflux tank, or the esterified steam is subjected to vapor-liquid separation through a flash evaporation tank, and the condensate water is returned to the reflux tank, or the esterified steam is subjected to low-level ORC power generation and utilization.
Disclosure of Invention
The utility model aims to solve the problems that in the conventional ORC waste heat recovery system, only steam and a cooling medium are subjected to low-degree heat exchange, and then steam condensate water is led back to a storage tank through a device or directly discharged to cause resource waste, and the problem that the prior ORC waste heat recovery system is insufficient is solved, and provides an esterification steam condensate water waste heat recovery device for ORC cascade utilization.
In order to achieve the above object, the present utility model adopts the following technical scheme:
an ORC cascade utilization esterification steam condensate water waste heat recovery device comprises an evaporator and an ethylene glycol separation tower; one end of the evaporator is connected with the glycol separation tower through a pipeline, and the evaporator further comprises a steam preheater, a condensate tank and a heat regenerator; the evaporator is connected with the steam preheater through a first pipeline and a second pipeline, and the evaporator is connected with the condensate tank through a third pipeline; the steam preheater is connected with the condensate tank through a fourth pipeline and a fifth pipeline, the steam preheater is connected with the condensate preheater through a sixth pipeline, and the condensate preheater is connected with the condensate tank through a seventh pipeline; the condensate preheater is connected with the heat regenerator through an eighth pipeline, and is connected with the downstream process section through a ninth pipeline;
the method comprises the steps that the esterified steam and non-condensable gas flowing out of an ethylene glycol separation tower enter an evaporator, an organic working medium flows through an eighth pipeline, a condensed water preheater, a sixth pipeline, a steam preheater and a first pipeline from a heat regenerator and flows into the evaporator, and the esterified steam exchanges heat with the organic working medium to form first steam condensate water and first incompletely cooled esterified steam containing the non-condensable gas;
the first steam condensate flows out of the evaporator and flows into the condensate tank through a third pipeline; the first incompletely cooled esterified steam containing non-condensable gas flows out of the evaporator, flows into the steam preheater through a second pipeline, exchanges heat with organic working medium in the steam preheater to form second steam condensate water and second incompletely cooled esterified steam containing non-condensable gas;
the second steam condensate flows out of the steam preheater, flows into the condensate tank through a fifth pipeline, and the second incompletely cooled esterified steam containing non-condensable gas flows into the condensate tank through a fourth pipeline;
the first steam condensate water and the second steam condensate water in the condensate tank flow into the bottom of the condensate tank under the action of gravity, flow into the condensate preheater through a seventh pipeline, exchange heat with organic working media in the condensate preheater to form condensate water, flow out of the condensate preheater through a ninth pipeline, flow into a downstream process section, and finish the cascade utilization of esterified steam and the recovery cycle of the waste heat of the steam condensate water.
As a further preferable aspect of the present utility model, a heat source regulating valve, a heat source pressure sensor, and a heat source temperature sensor are provided in this order between the glycol separation column and the evaporator.
As a further preferable mode of the utility model, the third pipeline and the fifth pipeline are both provided with U-shaped bends, and the fourth pipeline is provided with a stop valve.
As a further preferable mode of the utility model, the descending height of the U-shaped bend is more than or equal to 1m and less than or equal to 2 m, and a drain valve is arranged at the bottom of the U-shaped bend.
As a further preferred aspect of the present utility model, the ninth pipe is provided with a condensate water pressure sensor, a condensate water temperature sensor, and a condensate water flowmeter.
As a further preferable mode of the utility model, a reflux condenser is arranged at the upper part of the condensate tank, one end of the reflux condenser is connected with a fourth pipeline, the other end of the reflux condenser is connected with a cooling tower, and the top of the reflux condenser is connected with a non-condensable gas collecting tank through a pipeline; a flowmeter is arranged between the reflux condenser and the non-condensable gas collecting tank;
the cooling tower flows out of the cooling water, flows into the reflux condenser, and the second incompletely cooled esterified steam containing non-condensable gas flows into the reflux condenser through a fourth pipeline and exchanges heat with the cooling water in the reflux condenser to form third steam condensate water and non-condensable gas;
the non-condensable gas flows into the non-condensable gas collecting tank through a pipeline; the third steam condensate flows into the bottom of the condensate tank under the action of gravity.
As a further preferable mode of the utility model, a first branch and a second branch are arranged on the seventh pipeline in parallel, the first branch and the second branch have the same structure, a variable-frequency condensate pump is arranged on the first branch, a butterfly valve and a filter are arranged on one side of the variable-frequency condensate pump, which is close to the condensate tank, and a check valve, a butterfly valve and a second pressure gauge are arranged on one side of the variable-frequency condensate pump, which is close to the condensate preheater.
As a further preferable aspect of the present utility model, the liquid condensation tank is provided with a pressure gauge, a temperature gauge and a liquid level gauge.
As a further preferred aspect of the present utility model, there is also provided a generator, an expander, a water-cooled condenser and a working medium pump,
the evaporator is connected with the expansion machine through a tenth pipeline, the other end of the expansion machine is sequentially connected with the heat regenerator, the water-cooled condenser and one end of the working medium pump, a front filter is arranged between the working medium pump and the water-cooled condenser, and the other end of the working medium pump is connected with the heat regenerator; the water-cooled condenser is connected with the cooling tower;
the high-temperature gaseous organic working medium in the evaporator enters the expander through a tenth pipeline to do work, the expander drives the generator to generate power, the gaseous organic working medium after doing work flows out of the expander, flows through the regenerator and enters the water-cooled condenser, the cooling water in the cooling tower flows into the water-cooled condenser to exchange heat with the gaseous organic working medium, the liquid organic working medium is condensed into a liquid organic working medium, the liquid organic working medium enters the working medium pump, the liquid organic working medium in the water-cooled condenser is pumped back into the regenerator through the working medium pump to exchange heat with the gaseous organic working medium in the regenerator, and the liquid organic working medium after heat exchange flows into the condensed water preheater through the eighth pipeline to complete the ORC organic working medium power generation cycle.
As a further preferred aspect of the present utility model, the evaporator bottom is connected to the first pipe through an eleventh pipe.
Compared with the prior art, the esterification steam condensate water waste heat recovery device for ORC cascade utilization has the following beneficial effects:
1. the condensate tank is provided with a liquid level meter, a pressure gauge and a thermometer, so that the liquid level, the temperature and the pressure of steam condensate water in the condensate tank can be better detected;
2. a reflux condenser is arranged above the condensate tank, and the steam can be condensed into condensate water again through heat exchange between the steam and cooling water, so that the utilization rate of the steam is improved;
3. the non-condensable gas discharge pipeline and the flowmeter are designed above the condensate tank, so that the non-condensable gas from steam can be collected, the flow of the non-condensable gas can be measured and calculated, and the non-condensable gas discharge can be conveniently treated intensively by owners;
4. by designing the U-shaped bend in the pipeline, the problem that condensed water is pressed in the pipeline due to gas carried by steam condensed water from the steam preheater and the evaporator, so that the operation of the system is affected is solved;
5. the condensate pump is selected and is a variable frequency pump, and the variable frequency pump is added into a linkage control program of the system to control the liquid level of the condensate tank, so that the problem of how to enable the condensate tank to be at a proper liquid level to further improve the circulation efficiency of the system and the automatic control degree of the steam condensate recovery system is solved;
6. the two condensate pump branches are arranged, so that the problem that when the condensate pump fails, the condensate pump can be immediately switched to the other standby pump, and the operation of the main device of an owner is not influenced is solved;
7. the mode of connecting the evaporator shell side bottom with the evaporator working medium inlet pipeline is designed, so that the degree of participation of the organic working medium accumulated at the evaporator shell side bottom in circulation is improved;
8. by adopting the system design mode of the evaporator, the steam preheater, the condensate tank and the reflux condenser, on one hand, the purpose of cascade utilization of heat contained in the esterification steam as much as possible can be achieved, and on the other hand, the recovery efficiency of steam condensate water can be improved; from the aspect of economy, the utility model reduces the waste of heat of steam condensate to a certain extent, provides an integral design thought of waste heat recovery of esterified steam condensate by ORC cascade utilization, also provides a collection and measurement design thought of noncondensable gas in steam, improves the efficiency of an ORC waste heat power generation system, ensures the operation performance of MW-level ORC generator sets, increases sustainable power generation income, and reduces the operation cost, labor cost, transportation cost and the like of polyester workshops.
Drawings
FIG. 1 is a schematic flow diagram of an overall system for recovering waste heat of esterification steam condensate water for ORC cascade utilization of the utility model;
FIG. 2 is a schematic flow diagram of an esterification vapor ORC cascade utilization system;
FIG. 3 is a schematic flow diagram of a steam condensate waste heat utilization recovery system;
FIG. 4 is a schematic flow diagram of an ORC power cycle system.
Meaning of reference numerals in the drawings: 1. the device comprises an evaporator, 2, a steam preheater, 3, a condensate preheater, 4, a condensate tank, 5, a reflux condenser, 6, a variable-frequency condensate pump, 7, a flowmeter, 8, a regenerator, 9, a water-cooled condenser, 10, a pre-filter, 11, a working medium pump, 12, an expander, 13, a generator, 14, a heat source regulating valve, 15, a heat source pressure sensor, 16, a heat source temperature sensor, 17, a blow-down valve, 18, a stop valve, 19, a pressure gauge, 20, a thermometer, 21, a liquid level gauge, 22, a condensate pressure sensor, 23, a condensate temperature sensor, 24, a condensate flowmeter, 25, a first pipeline, 26, a second pipeline, 27, a third pipeline, 28, a fourth pipeline, 29, a fifth pipeline, 30, a sixth pipeline, 31, a seventh pipeline, 32, an eighth pipeline, 33, a ninth pipeline, 34, a tenth pipeline, 35 and an eleventh pipeline.
Detailed Description
The utility model is described in detail below with reference to the drawings and the specific embodiments.
As shown in FIG. 1, the esterification steam condensate water waste heat recovery device for ORC cascade utilization comprises an evaporator 1 and an ethylene glycol separation tower; one end of the evaporator 1 is connected with the glycol separation tower through a pipeline, and the evaporator also comprises a steam preheater 2, a condensate preheater 3, a condensate tank 4 and a heat regenerator 8; the evaporator 1 and the steam preheater 2 are connected through a first pipeline 25 and a second pipeline 26, and the evaporator 1 and the condensate tank 4 are connected through a third pipeline 27; the steam preheater 2 and the condensate tank 4 are connected through a fourth pipeline 28 and a fifth pipeline 29, the steam preheater 2 and the condensate preheater 3 are connected through a sixth pipeline 30, and the condensate preheater 3 and the condensate tank 4 are connected through a seventh pipeline 31; the condensate preheater 3 and the heat regenerator 8 are connected through an eighth pipeline 32, and the condensate preheater 3 is connected with a downstream process section through a ninth pipeline 33.
As shown in fig. 4, the bottom of the evaporator 1 is connected to the first pipe 25 through an eleventh pipe 35, and the liquid organic working medium accumulated in the bottom of the evaporator 1 enters the evaporator 1 along with the pipe.
A heat source regulating valve 14, a heat source pressure sensor 15 and a heat source temperature sensor 16 are sequentially arranged between the glycol separation tower and the evaporator 1.
The esterified steam and non-condensable gas flowing out of the glycol separation tower enter the evaporator 1, the organic working medium flows into the evaporator 1 from the heat regenerator 8 through an eighth pipeline 32, a condensate preheater 3, a sixth pipeline 30, a steam preheater 2 and a first pipeline 25, and the esterified steam exchanges heat with the organic working medium to form first steam condensate water and first incompletely cooled esterified steam containing the non-condensable gas.
As shown in fig. 2, the first steam condensate flows out of the evaporator 1, through a third conduit 27 into the condensate tank 4; the first non-fully cooled esterification vapor containing non-condensable gas flows out of the evaporator 1, flows into the vapor preheater 2 through the second pipeline 26, exchanges heat with organic working medium in the vapor preheater 2, and forms second vapor condensate and second non-fully cooled esterification vapor containing non-condensable gas.
The second steam condensate flows from the steam preheater 2 into the condensate tank 4 through a fifth conduit 29 and the second non-fully cooled esterification steam containing non-condensable gases flows into the condensate tank 4 through a fourth conduit 28.
U-shaped bends are arranged on the third pipeline 27 and the fifth pipeline 29, and a stop valve 18 is arranged on the fourth pipeline 28; the descending height of the U-shaped bend is more than or equal to 1m and less than or equal to 2 m, and a drain valve 17 is arranged at the bottom of the U-shaped bend.
As shown in fig. 3, a reflux condenser 5 is arranged at the upper part of the condensate tank 4, one end of the reflux condenser 5 is connected with a fourth pipeline 28, the other end is connected with a cooling tower, and the top of the reflux condenser 5 is connected with a non-condensable gas collecting tank through a pipeline; a flowmeter 7 is arranged between the reflux condenser 5 and the non-condensable gas collection tank.
Wherein, the cooling water flowing out of the cooling tower flows into the reflux condenser 5, the second incompletely cooled esterified steam containing non-condensable gas flows into the reflux condenser 5 through the fourth pipeline 28, and exchanges heat with the cooling water in the reflux condenser 5 to form third steam condensate water and non-condensable gas.
The non-condensable gas flows into the non-condensable gas collecting tank through a pipeline; the third steam condensate flows into the bottom of the condensate tank 4 under the action of gravity.
The first steam condensate water and the second steam condensate water in the condensate tank 4 flow into the bottom of the condensate tank 4 under the action of gravity, flow into the condensate preheater 3 through a seventh pipeline 31, exchange heat with organic working media in the condensate preheater 3 to form condensate water, flow out of the condensate preheater 3 through a ninth pipeline 33, flow into a downstream process section, and finish the cascade utilization of esterified steam and the waste heat recovery cycle of the steam condensate water.
As shown in fig. 2, a first branch and a second branch are connected in parallel on the seventh pipeline 31, the first branch and the second branch have the same structure, a variable-frequency condensate pump 6 is arranged on the first branch, a butterfly valve and a filter are arranged on one side of the variable-frequency condensate pump 6 close to the condensate tank 4, and a check valve, a butterfly valve and a second pressure gauge are arranged on one side of the variable-frequency condensate pump 6 close to the condensate preheater 3.
The pressure gauge 19, the thermometer 20 and the liquid level gauge 21 are arranged on the condensate tank 4, and the condensate tank 4 is also provided with a manhole, so that the inside of the condensate tank 4 can be better overhauled; the ninth pipe 33 is provided with a condensate water pressure sensor 22, a condensate water temperature sensor 23 and a condensate water flowmeter 24.
As shown in fig. 4, further comprises a generator 13, an expander 12, a water-cooled condenser 9 and a working medium pump 11,
the other end of the evaporator 1 is connected with an expander 12 through a tenth pipeline 34, the other end of the expander 12 is sequentially connected with one end of a heat regenerator 8, a water-cooled condenser 9 and a working medium pump 11, and a pre-filter 10 is arranged between the working medium pump 11 and the water-cooled condenser 9; the other end of the working medium pump 11 is connected with the heat regenerator 8; the water-cooled condenser 9 is connected to a cooling tower.
The high-temperature gaseous organic working medium in the evaporator 1 enters the expander 12 through a tenth pipeline 34 to do work, the expander 12 drives the generator 13 to generate power, the gaseous organic working medium after doing work flows out of the expander 12, flows through the regenerator 8 to enter the water-cooled condenser 9, cooling water in the cooling tower flows into the water-cooled condenser 9 to exchange heat with the gaseous organic working medium, and is condensed into a liquid organic working medium, the liquid organic working medium enters the working medium pump 11, the liquid organic working medium in the water-cooled condenser 9 is pumped back into the regenerator 8 through the working medium pump 11 to exchange heat with the gaseous organic working medium in the regenerator 8, and the liquid organic working medium after heat exchange flows into the condensate preheater 3 through an eighth pipeline 32 to complete the ORC organic working medium power generation cycle.
The foregoing has shown and described the basic principles, principal features and advantages of the utility model. It will be appreciated by persons skilled in the art that the above embodiments are not intended to limit the utility model in any way, and that all technical solutions obtained by means of equivalent substitutions or equivalent transformations fall within the scope of the utility model.
Claims (10)
1. An ORC cascade utilization esterification steam condensate water waste heat recovery device comprises an evaporator (1) and an ethylene glycol separation tower; one end of the evaporator (1) is connected with the glycol separation tower through a pipeline, and is characterized by further comprising a steam preheater (2), a condensate preheater (3), a condensate tank (4) and a heat regenerator (8); the evaporator (1) is connected with the steam preheater (2) through a first pipeline (25) and a second pipeline (26), and the evaporator (1) is connected with the condensate tank (4) through a third pipeline (27); the steam preheater (2) is connected with the condensate tank (4) through a fourth pipeline (28) and a fifth pipeline (29), the steam preheater (2) is connected with the condensate preheater (3) through a sixth pipeline (30), and the condensate preheater (3) is connected with the condensate tank (4) through a seventh pipeline (31); the condensate preheater (3) is connected with the heat regenerator (8) through an eighth pipeline (32), and the condensate preheater (3) is connected with a downstream process section through a ninth pipeline (33);
the method comprises the steps that esterified steam and non-condensable gas flowing out of an ethylene glycol separation tower enter an evaporator (1), organic working media flow through an eighth pipeline (32), a condensed water preheater (3), a sixth pipeline (30), a steam preheater (2) and a first pipeline (25) from a heat regenerator (8) and flow into the evaporator (1), the esterified steam exchanges heat with the organic working media to form first steam condensate water and first incompletely cooled esterified steam containing the non-condensable gas;
the first steam condensate flows out of the evaporator (1) and flows into the condensate tank (4) through a third pipeline (27); the first incompletely cooled esterified steam containing non-condensable gas flows out of the evaporator (1), flows into the steam preheater (2) through a second pipeline (26), exchanges heat with organic working medium in the steam preheater (2) to form second steam condensate and second incompletely cooled esterified steam containing non-condensable gas;
the second steam condensate flows out of the steam preheater (2), flows into the condensate tank (4) through a fifth pipeline (29), and the second incompletely cooled esterified steam containing non-condensable gas flows into the condensate tank (4) through a fourth pipeline (28);
the first steam condensate water and the second steam condensate water in the condensate tank (4) flow into the bottom of the condensate tank (4) under the action of gravity, flow into the condensate preheater (3) through a seventh pipeline (31), exchange heat with organic working media in the condensate preheater (3) to form condensate water, flow out of the condensate preheater (3) through a ninth pipeline (33) and flow into a downstream process section, and the cascade utilization of esterified steam and the recovery cycle of waste heat of the steam condensate water are completed.
2. The esterification steam condensate water waste heat recovery device for ORC cascade utilization according to claim 1, wherein a heat source regulating valve (14), a heat source pressure sensor (15) and a heat source temperature sensor (16) are sequentially arranged between the glycol separation tower and the evaporator (1).
3. The esterification steam condensate waste heat recovery device for ORC cascade utilization according to claim 1, wherein U-shaped bends are arranged on the third pipeline (27) and the fifth pipeline (29), and a stop valve (18) is arranged on the fourth pipeline (28).
4. The esterification steam condensate water waste heat recovery device for ORC cascade utilization according to claim 3, wherein the descending height of the U-shaped bend is more than or equal to 1m and less than or equal to 2 m, and a drain valve (17) is arranged at the bottom of the U-shaped bend.
5. The ORC cascade utilization esterification steam condensate waste heat recovery device according to claim 1, wherein the ninth pipe (33) is provided with a condensate water pressure sensor (22), a condensate water temperature sensor (23) and a condensate water flow meter (24).
6. The esterification steam condensate water waste heat recovery device for ORC cascade utilization according to claim 1, wherein a reflux condenser (5) is arranged at the upper part of the condensate tank (4), one end of the reflux condenser (5) is connected with a fourth pipeline (28), the other end of the reflux condenser is connected with a cooling tower, and the top of the reflux condenser (5) is connected with a non-condensable gas collecting tank through a pipeline; a flowmeter (7) is arranged between the reflux condenser (5) and the non-condensable gas collecting tank;
the cooling tower flows out of the cooling water, flows into the reflux condenser (5), and the second incompletely cooled esterified steam containing non-condensable gas flows into the reflux condenser (5) through a fourth pipeline (28) and exchanges heat with the cooling water in the reflux condenser (5) to form third steam condensate water and non-condensable gas;
the non-condensable gas flows into the non-condensable gas collecting tank through a pipeline; the third steam condensate water flows into the bottom of the condensate tank (4) under the action of gravity.
7. The esterification steam condensate water waste heat recovery device for ORC cascade utilization according to claim 1, wherein a first branch and a second branch are arranged on the seventh pipeline (31) in parallel, the first branch and the second branch are identical in structure, a variable-frequency condensate pump (6) is arranged on the first branch, a butterfly valve and a filter are arranged on one side, close to the condensate tank (4), of the variable-frequency condensate pump (6), and a check valve, a butterfly valve and a second pressure gauge are arranged on one side, close to the condensate preheater (3), of the variable-frequency condensate pump (6).
8. The device for recycling waste heat of esterification steam condensate water by ORC cascade utilization according to claim 1, wherein a pressure gauge (19), a thermometer (20) and a liquid level gauge (21) are arranged on the condensate tank (4).
9. The device for recycling the waste heat of the esterified steam condensate water by ORC cascade utilization according to claim 1, further comprising a generator (13), an expander (12), a water-cooled condenser (9) and a working medium pump (11),
the evaporator (1) is connected with the expander (12) through a tenth pipeline (34), the other end of the expander (12) is sequentially connected with the heat regenerator (8), the water-cooled condenser (9) and one end of the working medium pump (11), a front filter (10) is arranged between the working medium pump (11) and the water-cooled condenser (9), and the other end of the working medium pump (11) is connected with the heat regenerator (8); the water-cooled condenser (9) is connected with a cooling tower;
the high-temperature gaseous organic working medium in the evaporator (1) enters the expander (12) through a tenth pipeline (34) to do work, the expander (12) drives the generator (13) to generate power, the gaseous organic working medium after doing work flows out of the expander (12), flows through the regenerator (8) to enter the water-cooled condenser (9), the cooling water in the cooling tower flows into the water-cooled condenser (9) to exchange heat with the gaseous organic working medium, the liquid organic working medium is condensed into a liquid organic working medium, the liquid organic working medium enters the working medium pump (11), the liquid organic working medium in the water-cooled condenser (9) is pumped back into the regenerator (8) through the working medium pump (11) to exchange heat with the gaseous organic working medium in the regenerator (8), and the liquid organic working medium after exchanging heat flows into the condensed water preheater (3) through an eighth pipeline (32) to complete the ORC organic working medium power generation cycle.
10. The ORC cascade utilization esterification steam condensate waste heat recovery apparatus of claim 1, wherein the bottom of the evaporator (1) is connected to the first conduit (25) via an eleventh conduit (35).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202323062167.4U CN220206416U (en) | 2023-11-14 | 2023-11-14 | ORC cascade utilization's esterification steam condensate water waste heat recovery device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202323062167.4U CN220206416U (en) | 2023-11-14 | 2023-11-14 | ORC cascade utilization's esterification steam condensate water waste heat recovery device |
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| CN220206416U true CN220206416U (en) | 2023-12-19 |
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| CN202323062167.4U Active CN220206416U (en) | 2023-11-14 | 2023-11-14 | ORC cascade utilization's esterification steam condensate water waste heat recovery device |
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