CN203730205U - Two-stage permeation concentration difference working device driven by low-grade heat source - Google Patents
Two-stage permeation concentration difference working device driven by low-grade heat source Download PDFInfo
- Publication number
- CN203730205U CN203730205U CN201320837436.7U CN201320837436U CN203730205U CN 203730205 U CN203730205 U CN 203730205U CN 201320837436 U CN201320837436 U CN 201320837436U CN 203730205 U CN203730205 U CN 203730205U
- Authority
- CN
- China
- Prior art keywords
- liquid
- pressure
- low
- chamber
- pressure energy
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn - After Issue
Links
Landscapes
- Engine Equipment That Uses Special Cycles (AREA)
Abstract
The utility model discloses a two-stage permeation concentration difference working device driven by a low-grade heat source. The two-stage permeation concentration difference working device comprises a generator and others. The generator is connected with a condenser. The condenser is connected with a low-pressure chamber liquid cavity I and a low-pressure chamber liquid cavity II. The generator is connected with a solution heat exchanger connected with a first pressure energy recovery device, and the first pressure energy recovery device is connected with an inlet of the high-pressure chamber liquid cavity I. An outlet of the high-pressure chamber liquid cavity I is respectively connected with the first pressure energy recovery device and a liquid inlet of a first liquid turbine. A high-pressure liquid pipeline of the first pressure energy recovery device and a liquid outlet of the first liquid turbine are respectively connected with a second pressure energy recovery device, and the second pressure energy recovery device is connected with an inlet of a high-pressure chamber liquid cavity II. An outlet of the high-pressure chamber liquid cavity II is respectively connected with the second pressure energy recovery device and a liquid inlet of a second liquid turbine. The second pressure energy recovery device is connected with the solution heat exchanger, and the solution heat exchanger and a liquid outlet of the second liquid turbine are respectively connected with the generator.
Description
Technical field
The utility model relates to power equipment technical field, the two-stage infiltration concentration difference acting device that specifically a kind of low-grade heat source drives.
Background technique
Concentration difference acting comes across in seawater utilization engineering conventionally, and its essence is to utilize the difference in chemical potential acting having between seawater and freshwater, conventionally can realize by osmometry and vapor pressure method; Vapor pressure method is to allow the different solution of concentration evaporate under balance pressure separately, concentration difference can be converted to gas pressure energy, and reclaim by steam turbine; Osmometry is to allow the different solution of concentration carry out matter exchange by selectivity semipermeable membrane, and concentration difference can be converted to fluid pressure energy, and utilizes liquid turbine machine to reclaim.Therefore because obtained fluid pressure differential is far above gas differential pressure, in the situation that concentration difference can be very little (concentration difference is less than 1%), also can utilize osmometry to reclaim the concentration difference energy between seawater and fresh water.
When utilizing osmometry to carry out concentration difference when acting, first need to solve have certain concentration difference solution carry out source problem, in coastal area, adopt seawater and fresh water natural resources no doubt convenient, but to vast hinterland obviously and inapplicable.A kind of feasible mode is that the low-grade heat source (<100 ℃) that utilization extensively exists is that driving force is regenerated to the dilute solution after doing work, form an enclosed power circulation system, form the energy transfer process of heat energy-concentration difference energy-fluid pressure energy-merit.
Under the overall background of energy-conserving and environment-protective, the power cycle that adopts low-grade heat source to drive has obtained increasing attention and application in recent years, but current power cycle is nearly all to adopt vapor pressure method, is the energy transfer process of heat energy-gas pressure energy-merit.Although on energy transmits, vapor pressure method is than the few link of osmometry, but as previously mentioned, the gas differential pressure that vapor pressure method obtains is much smaller than the fluid pressure differential of osmometry, therefore when between driving heat source and ambient temperature, the temperature difference is very little (as 20 ℃～30 ℃), the efficiency that adopts vapor pressure method to promote steam turbine acting will sharply reduce and lose Technological Economy value.Even if adopt the normal screw type decompressor that adopts in organic rankie cycle generating at present, be generally also difficult to utilize 80 ℃ of following thermals source, more impossible under 20 ℃～30 ℃ temperature difference normal, efficient operation.
As can be seen here, osmometry concentration difference acting device is particularly suitable for driving with the low-grade heat source of lower temperature, this type systematic at first by American scholar last century the mid-1970s propose, the initial stage eighties has added again pressure energy recovering device conventional in reverse osmosis unit further to improve system effectiveness.In use still there is following narrow limitation in this type systematic at present: 1, adopt single-stage infiltration, when systemic circulation multiplying power is higher, by the losses by mixture obviously increasing in process of osmosis; 2, the working medium of using is saline solution, in the regenerative process of water after driven liquid absorbs, the heat consuming is larger, has reduced system thermal efficiency, in addition under certain osmotic pressure, required heat source temperature level is too low, in fact can increase the proportion of temperature difference heat exchange in irreversible loss, and under certain heat source temperature, adopting the aqueous solution is the working medium as easy as rolling off a log withstand voltage limit that makes osmotic pressure substantially exceed semipermeable membrane again.
In sum, necessary existing osmometry concentration difference acting device is improved, make it to have the higher thermal efficiency and acting ability.
Model utility content
The technical problems to be solved in the utility model is to provide the two-stage infiltration concentration difference acting device that a kind of low-grade heat source simple in structure drives.
In order to solve the problems of the technologies described above, the two-stage infiltration concentration difference acting device that the utility model provides a kind of low-grade heat source to drive, comprises generator, condenser, the first permeate chamber, solution heat exchanger, the first pressure energy recover, first liquid turbine, the second permeate chamber, the second pressure energy recover and second liquid turbine; The gas outlet of described generator is connected with the condensation pipe of condenser; The condensation pipe of described condenser is connected with the low pressure chamber liquid container I of the first permeate chamber and the low pressure chamber liquid container II of the second permeate chamber respectively; The liquid outlet of described generator is connected with one end of the high-temp liquid pipeline of solution heat exchanger, other one end of the high-temp liquid pipeline of solution heat exchanger is connected with one end of the low pressure liquid pipeline of the first pressure energy recover, and other one end of the low pressure liquid pipeline of the first pressure energy recover is connected with the hyperbaric chamber liquid container I entrance of the first permeate chamber; The hyperbaric chamber liquid container I outlet of the first permeate chamber is connected with highly pressurised liquid pipeline one end of the first pressure energy recover and the liquid inlet of first liquid turbine I respectively; Other one end of the highly pressurised liquid pipeline of the first pressure energy recover is connected with low pressure liquid pipeline one end of the second pressure energy recover respectively with the liquid outlet of first liquid turbine I, and other one end of low pressure liquid pipeline of the second pressure energy recover is connected with the hyperbaric chamber liquid container II entrance of the second permeate chamber; The hyperbaric chamber liquid container II outlet of the second permeate chamber is connected with highly pressurised liquid pipeline one end of the second pressure energy recover and the liquid inlet of first liquid turbine II respectively; The highly pressurised liquid pipeline the other end of described the second pressure energy recover is connected with one end of the low-temperature liquid pipe of solution heat exchanger, and other one end of the low-temperature liquid pipe of solution heat exchanger is connected with the liquid inlet of generator respectively with the liquid outlet of first liquid turbine II.
Improvement as the two-stage infiltration concentration difference acting device that low-grade heat source described in the utility model is driven: be provided with the first suction booster between the hyperbaric chamber liquid container I entrance of other one end of the low pressure liquid pipeline of described the first pressure energy recover and the first permeate chamber; Between the hyperbaric chamber liquid container II entrance of other one end of low pressure liquid pipeline of described the second pressure energy recover and the second permeate chamber, be provided with the second suction booster; Between low pressure liquid pipeline one end of the liquid outlet of described first liquid turbine I and the second pressure energy recover, be provided with the first pressure regulator valve; Between the liquid outlet of described first liquid turbine II and the liquid inlet of generator, be provided with the second pressure regulator valve; Between other one end of the low-temperature liquid pipe of described solution heat exchanger and the liquid inlet of generator, be provided with the 3rd pressure regulator valve; Between low pressure liquid pipeline one end of other one end of the highly pressurised liquid pipeline of described the first pressure energy recover and the second pressure energy recover, be provided with the 4th pressure regulator valve.
Further improvement as the two-stage infiltration concentration difference acting device that low-grade heat source described in the utility model is driven: be provided with semipermeable membrane I between the low pressure chamber liquid container I of described the first permeate chamber and hyperbaric chamber liquid container I; Between the low pressure chamber liquid container II of described the second permeate chamber and hyperbaric chamber liquid container II, be provided with semipermeable membrane II.
Further improvement as the two-stage infiltration concentration difference acting device that low-grade heat source described in the utility model is driven: organic mixed working fluid that the built-in high boiling component of described generator and low boiling component are mixed; Described semipermeable membrane I and semipermeable membrane II are can be by the low boiling component in organic mixed working fluid, and can not see through film by the selectivity of high boiling component.
Further improvement as the two-stage infiltration concentration difference acting device that low-grade heat source described in the utility model is driven: described the first suction booster and the second suction booster are variable frequency pump.
The using method step of the two-stage infiltration concentration difference acting device that low-grade heat source described in the utility model drives is as follows: the first step: by the heating of mixed working fluid solution, produce low boiling component steam I and concentrated solution I; Second step: low boiling component steam I becomes low boiling component liquid I after condensation; The 3rd step: concentrated solution I, after heat release cooling and absorption pressure energy, is mixed into dilute solution I with a part of low boiling component liquid I; On the one hand, dilute solution I release pressure absorbs to concentrated solution I; In addition on the one hand, dilute solution I driving power device I outputting power; The 4th step: after two dilute solution I of step 3 are mixed, absorption pressure energy, and be mixed into dilute solution II with other a part of low boiling component liquid I; On the one hand, the mixed solution of two dilute solution I of dilute solution II release pressure energy step 3 absorbs, and absorbs the heat of concentrated solution I, makes the concentrated solution I cooling in step 2; In addition on the one hand, dilute solution II driving power device II outputting power.
The infiltration concentration difference acting device that the utility model drives with existing low-grade heat source is compared, and has the following advantages:
1) with organic mixed working fluid, replace the aqueous solution, can reduce heat that separation process consumes, improve heat source temperature, reduce osmotic pressure, thereby be conducive to increase system thermal efficiency, reduce the proportion of temperature difference heat exchange in irreversible loss and reduce the requirement of withstand voltage to semipermeable membrane.
2) adopt two-stage infiltration, be conducive to, by when reducing circulating ratio saving suction booster energy consumption, avoid producing larger irreversible losses by mixture, make system there is larger acting ability.
Accompanying drawing explanation
Below in conjunction with accompanying drawing, embodiment of the present utility model is described in further detail.
Fig. 1 is main structure schematic diagram of the present utility model.
Embodiment
Embodiment 1, Fig. 1 have provided the two-stage infiltration concentration difference acting device that a kind of low-grade heat source drives; Comprise generator 1, condenser 2, the first permeate chamber 3, solution heat exchanger 4, the first pressure energy recover 5, the first suction booster 6, first liquid turbine 7, the first pressure regulator valve 8, the second permeate chamber 9, the second pressure energy recover 10, the second suction booster 11, second liquid turbine 12, the second pressure regulator valve 13, the 3rd pressure regulator valve 14 and the 4th pressure regulator valve 15.
The gas outlet of generator 1 is connected with the condensation pipe of condenser 2; The condensation pipe of condenser 2 is connected with the low pressure chamber liquid container I 31 of the first permeate chamber 3 and the low pressure chamber liquid container II 91 of the second permeate chamber 9 respectively; The liquid outlet of generator 1 is connected with one end of the high-temp liquid pipeline of solution heat exchanger 4, other one end of the high-temp liquid pipeline of solution heat exchanger 4 is connected with one end of the low pressure liquid pipeline of the first pressure energy recover 5, and other one end of the low pressure liquid pipeline of the first pressure energy recover 5 is connected with hyperbaric chamber liquid container I 32 entrances of the first permeate chamber 3; Hyperbaric chamber liquid container I 32 outlets of the first permeate chamber 3 are connected with highly pressurised liquid pipeline one end of the first pressure energy recover 5 and the liquid inlet of first liquid turbine 7 respectively; Other one end of the highly pressurised liquid pipeline of the first pressure energy recover 5 is connected with low pressure liquid pipeline one end of the second pressure energy recover 10 respectively with the liquid outlet of first liquid turbine 7 I, and other one end of low pressure liquid pipeline of the second pressure energy recover 10 is connected with hyperbaric chamber liquid container II 92 entrances of the second permeate chamber 9; Hyperbaric chamber liquid container II 92 outlets of the second permeate chamber 9 are connected with highly pressurised liquid pipeline one end of the second pressure energy recover 10 and the liquid inlet of second liquid turbine 12 respectively; The highly pressurised liquid pipeline the other end of the second pressure energy recover 10 is connected with one end of the low-temperature liquid pipe of solution heat exchanger 4, and other one end of the low-temperature liquid pipe of solution heat exchanger 4 is connected with the liquid inlet of generator 1 respectively with the liquid outlet of second liquid turbine 12.
Between hyperbaric chamber liquid container I 32 entrances of other one end of the low pressure liquid pipeline of the first pressure energy recover 5 and the first permeate chamber 3, the first suction booster 6 is set; Between hyperbaric chamber liquid container II 92 entrances of other one end of low pressure liquid pipeline of the second pressure energy recover 10 and the second permeate chamber 9, the second suction booster 11 is set; Between low pressure liquid pipeline one end of the liquid outlet of first liquid turbine 7 I and the second pressure energy recover 10, the first pressure regulator valve 8 is set; The second pressure regulator valve 13 is set between the liquid inlet of the liquid outlet of second liquid turbine 12 and generator 1; Between other one end of the low-temperature liquid pipe of solution heat exchanger 4 and the liquid inlet of generator 1, the 3rd pressure regulator valve 14 is set; Between low pressure liquid pipeline one end of other one end of the highly pressurised liquid pipeline of the first pressure energy recover 5 and the second pressure energy recover 10, the 4th pressure regulator valve 15 is set.
Between the low pressure chamber liquid container I 31 of the first permeate chamber 3 and hyperbaric chamber liquid container I 32, be provided with semipermeable membrane I 16; Between the low pressure chamber liquid container II 91 of the second permeate chamber 9 and hyperbaric chamber liquid container II 92, be provided with semipermeable membrane II 17.
Organic mixed working fluid that the built-in high boiling component of generator 1 and low boiling component are mixed, this organic mixed working fluid has height intersolubility and less separated latent heat, and the boiling point between high boiling component and low boiling component differs larger, high boiling component is evaporated hardly, solution surface vapor tension is determined by the vapor tension of low boiling component, the critical temperature of low boiling component and ambient temperature differ should be 100 ℃ of left and right, to guarantee compared with little gas, liquid density difference and to avoid osmotic pressure excessive.Semipermeable membrane I 16 and semipermeable membrane II 17 are can be by the low boiling component in organic mixed working fluid, and can not see through film by the selectivity of high boiling component.The first suction booster 6 and the second suction booster 11 are variable frequency pump, can set and regulate according to outlet pressure.The merit of exporting by first liquid turbine 7 and second liquid turbine 12 can be for directly promoting mechanical rotation or driving generator to generate electricity.The low-grade heat source of the utility model utilization comprises solar energy, thermal gradient energy of sea water and various industrial exhaust heat, and its temperature levels should be within the scope of higher than 20 ℃～50 ℃ of ambient temperatures.
When in organic mixed working fluid steam, amount of components having low boiling points is not high, a kind of preferred technological scheme is: with rectifier, replace generator 1, low boiling component is carried out to rectifying to reach higher purity.
In the time of concrete use, step is as follows:
1, utilize external heat source to the mixed working fluid solution heating in generator 1, make a part of low boiling component wherein be subject to thermal evaporation, produce low boiling component steam I; The low boiling component steam I and the concentrated solution I (unevaporated part is concentrated solution I after heating) that produce are divided into two-way, flow out respectively from gas outlet and the liquid outlet of generator 1.
2, the concentrated solution I flowing out from the liquid outlet of generator 1 enters the high-temp liquid pipeline of solution heat exchanger 4, emit (the liquid absorption heat in the low-temperature liquid pipe of solution heat exchanger 4 after heat, refer to step 8), temperature reduces, enter again the low pressure liquid pipeline of the first pressure energy recover 5, the high-pressure solution absorbing in highly pressurised liquid pipeline (in the first pressure energy recover 5) (refers to the pressure energy that step 5) discharges, after raising, pressure further boosts to hyperbaric chamber liquid container I 32 inlet pressures of the first permeate chamber 3 by the first suction booster 6, and flow into from hyperbaric chamber liquid container I 32 entrances.
3, the low boiling component steam I flowing out from generator 1 gas outlet enters condenser 2, and by external source, be condensed into low boiling component liquid I in the condensation pipe of condenser 2, simultaneous temperature reduces, low boiling component liquid I is divided into two-way from condensation pipe flows out, wherein a road flows into the low pressure chamber liquid container I 31 of the first permeate chamber 3, and an other road flows into the low pressure chamber liquid container II 91 of the second permeate chamber 9.
4, the low boiling component liquid I in the low pressure chamber liquid container I 31 of the first permeate chamber 3 enters hyperbaric chamber liquid container I 32 by semipermeable membrane I 16 under the driving of semipermeable membrane I 16 both sides Liquid Penetrant pressure reduction, the concentrated solution I flowing into hyperbaric chamber liquid container I 32 entrances becomes dilute solution I after mixing, then flows out from 32 outlets of hyperbaric chamber liquid container I.
5, the dilute solution I flowing out from hyperbaric chamber liquid container I 32 outlets of the first permeate chamber 3 is divided into two-way:
Wherein a road enters the liquid inlet of first liquid turbine 7, and release pressure can promote liquid turbine and externally do work, and passes through the outlet pressure of the first pressure regulator valve 8 pressure regulation to the four pressure regulator valves 15 after pressure decreased again;
An other road enters the highly pressurised liquid pipeline of the first pressure energy recover 5, release pressure can be (in step 2, concentrated solution I enters the high-temp liquid pipeline of solution heat exchanger 4, emit after heat, temperature reduces, then enters the low pressure liquid pipeline of the first pressure energy recover 5, absorbs the pressure energy that the first pressure energy recover 5 inner high voltage fluid pipelines discharge) after, pressure decreased, then pass through the 4th pressure regulator valve 15 pressure regulation to the outlet pressure of the first pressure regulator valve 8.
6, the dilute solution I that the dilute solution I flowing out from the first pressure regulator valve 8 and the 4th pressure regulator valve 15 flow out enters the low pressure liquid pipeline of the second pressure energy recover 10 again mutually mixing, the high-pressure solution absorbing in highly pressurised liquid pipeline (in the second pressure energy recover 10) (refers to the pressure energy that step 8) discharges, pressure raises, by the second suction booster 11, further boost to again hyperbaric chamber liquid container II 92 inlet pressures of the second permeate chamber 9, and flow into from hyperbaric chamber liquid container II 92 entrances.
7, the low boiling component liquid I in the low pressure chamber liquid container II 91 of the second permeate chamber 9 is under the driving of semipermeable membrane II 17 both sides Liquid Penetrant pressure reduction, by semipermeable membrane II 17, enter hyperbaric chamber liquid container II 92, the solution flowing into hyperbaric chamber liquid container II 92 entrances from the second permeate chamber 9 is (step 6, the dilute solution I that the dilute solution I flowing out from the first pressure regulator valve 8 and the 4th pressure regulator valve 15 flow out is mixed mutually) become dilute solution II mixing, then flow out from 92 outlets of hyperbaric chamber liquid container II.
8, the dilute solution II flowing out from hyperbaric chamber liquid container II 92 outlets of the second permeate chamber 9 is divided into two-way:
Wherein a road enters second liquid turbine II 12, and release pressure can promote liquid turbine and externally do work, and after pressure decreased, is depressured to generator pressure again by the second pressure regulator valve 13;
An other road enters the highly pressurised liquid pipeline of the second pressure energy recover 10, after release pressure energy, pressure decreased is (in step 6, the mutual mixed solution absorption pressure energy of dilute solution I that the dilute solution I flowing out from the first pressure regulator valve 8 and the 4th pressure regulator valve 15 flow out), and then enter the low-temperature liquid pipe of solution heat exchanger 4, absorb pyrosol (in step 2, the concentrated solution I flowing out from the liquid outlet of generator 1 enters heat release the high-temp liquid pipeline of solution heat exchanger 4) after the heat that discharges, temperature raises, by the 3rd pressure regulator valve 14, be depressured to generator 1 pressure again.
9, the solution flowing out from the second pressure regulator valve 13, the 3rd pressure regulator valve 14 flows into generator 1 from the liquid-inlet of generator 1 after mixing (referring to step 8, the dilute solution II that the dilute solution II that wherein the second pressure regulator valve 13 flows out and the 3rd pressure regulator valve 14 flow out) again.
The calculating parameter of embodiment 1 in Table 1(for 1kg condensator outlet liquid working substance R134a).Design condition is: 32 ℃ of ambient temperatures, infiltration acting working medium is that R134a(can pass through semipermeable membrane), driving heat source temperature is 65.3 ℃, condensation Subcoold temperature is 2 ℃, circulating ratio is 2.5, and recuperator, liquid turbine, solution heat exchanger efficiency are respectively 95%, 90%, 70%.The thermal efficiency that embodiment 1 calculates (being defined as the ratio of liquid turbine output work and suction booster input work difference and thermal source heat consumption) is 2.64%, the reason that this value is lower is that heat source temperature and ambient temperature have a narrow range of temperature, the thermodynamic theories value of the thermal efficiency is also only less than 10%, but the system calculating fire (is defined as the showing tremendous enthusiasm ratio of using that liquid turbine output work and suction booster input work difference and thermal source provide) with imitating, reaches 26.8%.Compare (in Table 1 secondary series) with existing infiltration concentration difference acting device, embodiment 1, under identical operating mode, adopts the rear thermal efficiency of two-stage infiltration and system fire all to improve 19.5% by efficiency, and effectively output work has increased by 20.3%.In addition, the utility model adopt to mix organic working medium, and comparing glassware for drinking water has and more have the less latent heat of vaporization, as the latent heat of vaporization of R134a is about 160kJ/kg, less than 1/10 of water vapor latent heat, therefore in regenerative process, can greatly save heat consumption, improves system thermal efficiency.
As can be seen here, the utility model is compared existing infiltration concentration difference working system and is had the higher thermal efficiency and acting ability, has effectively realized original intention of the present utility model.
In above embodiment, can consider the factors such as concrete service condition and requirement, technical and economic performance and rationally determine the design parameter of system, to take into account applicability and the Economy of system.
The heating power result of calculation of table 1 embodiment 1 (for 1kg condensator outlet liquid working substance R134a)
Finally, it is also to be noted that, what more than enumerate is only several specific embodiments of the present utility model.Obviously, the utility model is not limited to above embodiment, can also have many distortion.All distortion that those of ordinary skill in the art can directly derive or associate from the disclosed content of the utility model, all should think protection domain of the present utility model.
Claims (5)
1. the two-stage infiltration concentration difference acting device that low-grade heat source drives, comprises generator (1), condenser (2), the first permeate chamber (3), solution heat exchanger (4), the first pressure energy recover (5), first liquid turbine (7), the second permeate chamber (9), the second pressure energy recover (10) and second liquid turbine (12); It is characterized in that: the gas outlet of described generator (1) is connected with the condensation pipe of condenser (2); The condensation pipe of described condenser (2) is connected with the low pressure chamber liquid container I (31) of the first permeate chamber (3) and the low pressure chamber liquid container II (91) of the second permeate chamber (9) respectively;
The liquid outlet of described generator (1) is connected with one end of the high-temp liquid pipeline of solution heat exchanger (4), other one end of the high-temp liquid pipeline of solution heat exchanger (4) is connected with one end of the low pressure liquid pipeline of the first pressure energy recover (5), and other one end of the low pressure liquid pipeline of the first pressure energy recover (5) is connected with hyperbaric chamber liquid container I (32) entrance of the first permeate chamber (3);
Hyperbaric chamber liquid container I (32) outlet of the first permeate chamber (3) is connected with highly pressurised liquid pipeline one end of the first pressure energy recover (5) and the liquid inlet of first liquid turbine (7) respectively; Other one end of the highly pressurised liquid pipeline of the first pressure energy recover (5) is connected with low pressure liquid pipeline one end of the second pressure energy recover (10) respectively with the liquid outlet of first liquid turbine (7), and other one end of low pressure liquid pipeline of the second pressure energy recover (10) is connected with hyperbaric chamber liquid container II (92) entrance of the second permeate chamber (9);
Hyperbaric chamber liquid container II (92) outlet of the second permeate chamber (9) is connected with highly pressurised liquid pipeline one end of the second pressure energy recover (10) and the liquid inlet of second liquid turbine (12) respectively; The highly pressurised liquid pipeline the other end of described the second pressure energy recover (10) is connected with one end of the low-temperature liquid pipe of solution heat exchanger (4), and other one end of the low-temperature liquid pipe of solution heat exchanger (4) is connected with the liquid inlet of generator (1) respectively with the liquid outlet of second liquid turbine (12).
2. the two-stage infiltration concentration difference acting device that low-grade heat source according to claim 1 drives, is characterized in that: between hyperbaric chamber liquid container I (32) entrance of other one end of the low pressure liquid pipeline of described the first pressure energy recover (5) and the first permeate chamber (3), be provided with the first suction booster (6);
Between hyperbaric chamber liquid container II (92) entrance of other one end of low pressure liquid pipeline of described the second pressure energy recover (10) and the second permeate chamber (9), be provided with the second suction booster (11);
Between low pressure liquid pipeline one end of the liquid outlet of described first liquid turbine (7) I and the second pressure energy recover (10), be provided with the first pressure regulator valve (8);
Between the liquid inlet of the liquid outlet of described second liquid turbine (12) and generator (1), be provided with the second pressure regulator valve (13);
Between the liquid inlet of other one end of the low-temperature liquid pipe of described solution heat exchanger (4) and generator (1), be provided with the 3rd pressure regulator valve (14);
Between low pressure liquid pipeline one end of other one end of the highly pressurised liquid pipeline of described the first pressure energy recover (5) and the second pressure energy recover (10), be provided with the 4th pressure regulator valve (15).
3. the two-stage infiltration concentration difference acting device that low-grade heat source according to claim 2 drives, is characterized in that: between the low pressure chamber liquid container I (31) of described the first permeate chamber (3) and hyperbaric chamber liquid container I (32), be provided with semipermeable membrane I (16);
Between the low pressure chamber liquid container II (91) of described the second permeate chamber (9) and hyperbaric chamber liquid container II (92), be provided with semipermeable membrane II (17).
4. the two-stage infiltration concentration difference acting device that low-grade heat source according to claim 3 drives, is characterized in that: organic mixed working fluid that the built-in high boiling component of described generator (1) and low boiling component are mixed;
Described semipermeable membrane I (16) and semipermeable membrane II (17) are can be by the low boiling component in organic mixed working fluid, and can not see through film by the selectivity of high boiling component.
5. the two-stage infiltration concentration difference acting device that low-grade heat source according to claim 4 drives, is characterized in that: described the first suction booster (6) and the second suction booster (11) are variable frequency pump.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320837436.7U CN203730205U (en) | 2013-12-17 | 2013-12-17 | Two-stage permeation concentration difference working device driven by low-grade heat source |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320837436.7U CN203730205U (en) | 2013-12-17 | 2013-12-17 | Two-stage permeation concentration difference working device driven by low-grade heat source |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203730205U true CN203730205U (en) | 2014-07-23 |
Family
ID=51200284
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201320837436.7U Withdrawn - After Issue CN203730205U (en) | 2013-12-17 | 2013-12-17 | Two-stage permeation concentration difference working device driven by low-grade heat source |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203730205U (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103726975A (en) * | 2013-12-17 | 2014-04-16 | 浙江理工大学 | Low-grade heat source driven and two-stage infiltration adopted concentration difference working device and method |
| CN104848596A (en) * | 2015-04-24 | 2015-08-19 | 浙江理工大学 | Membrane type thermal power circulating device and method adopting low-grade heat source |
| CN110146606A (en) * | 2019-05-06 | 2019-08-20 | 北京水木滨华科技有限公司 | A kind of preprocess method of highly pressurised liquid component |
| CN111795514A (en) * | 2020-06-16 | 2020-10-20 | 普泛能源技术研究院(北京)有限公司 | Absorption type heat exchange circulating system |
-
2013
- 2013-12-17 CN CN201320837436.7U patent/CN203730205U/en not_active Withdrawn - After Issue
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103726975A (en) * | 2013-12-17 | 2014-04-16 | 浙江理工大学 | Low-grade heat source driven and two-stage infiltration adopted concentration difference working device and method |
| CN104848596A (en) * | 2015-04-24 | 2015-08-19 | 浙江理工大学 | Membrane type thermal power circulating device and method adopting low-grade heat source |
| CN110146606A (en) * | 2019-05-06 | 2019-08-20 | 北京水木滨华科技有限公司 | A kind of preprocess method of highly pressurised liquid component |
| CN111795514A (en) * | 2020-06-16 | 2020-10-20 | 普泛能源技术研究院(北京)有限公司 | Absorption type heat exchange circulating system |
| CN111795514B (en) * | 2020-06-16 | 2021-04-06 | 普泛能源技术研究院(北京)有限公司 | Absorption type heat exchange circulating system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102213199B (en) | Method and device for utilizing ocean temperature difference to generate electricity | |
| CN110344898B (en) | Absorption type sea water desalination and closed cycle power generation system | |
| WO2019114536A1 (en) | Constructed cold source energy recovery system, heat engine system and energy recovery method | |
| CN102434235A (en) | Kalina cycle generation system adopting ejector | |
| CN101666250A (en) | System for improving low-temperature heat source power generation capacity by using injection pump | |
| CN203730205U (en) | Two-stage permeation concentration difference working device driven by low-grade heat source | |
| CN112554983A (en) | Liquid carbon dioxide energy storage system and method coupled with kalina cycle | |
| CN103090582B (en) | The absorption energy storage equipment of a kind of boosting type three-phase | |
| CN205297661U (en) | Take waste heat power generation system of calorimeter back to | |
| CN103726975B (en) | The two-stage infiltration concentration difference acting device and method that low-grade heat source drives | |
| CN110986418B (en) | Absorption type circulating system based on temperature rising and pressure rising technology | |
| CN110697821B (en) | Seawater source trans-critical carbon dioxide heat pump circulation multi-effect seawater desalination system | |
| CN210317415U (en) | Absorption type seawater desalination and closed cycle power generation system | |
| CN110259537B (en) | Carbon dioxide Rankine cycle power system and operation method thereof | |
| CN104848596B (en) | Membrane type thermodynamic circulation device and method using low-grade heat source | |
| WO2023083242A1 (en) | Low-temperature cyclic power generation system and method with carbon dioxide gas as working medium | |
| CN103175332A (en) | Two-stage absorption refrigeration circulation system based on double working pairs and refrigeration method thereof | |
| CN107630727B (en) | Medium-low temperature heat energy driven power generation, refrigeration and carbon capture coupling system | |
| CN103994599A (en) | Transcritical injection refrigeration system based on gas-liquid injection pump | |
| CN110567189B (en) | Vapor compression type absorption heat pump | |
| CN110243009B (en) | Absorption heat pump heat storage and release system for heat supply unit and working method thereof | |
| CN209875221U (en) | System for improving power generation capacity of medium-low temperature heat source by adopting injection pump and separator | |
| CN112412560A (en) | Kalina circulation system based on single screw expander | |
| CN112576328A (en) | Power cycle water and electricity cogeneration system and method thereof | |
| CN111121339A (en) | Industrial waste heat or geothermal energy and air energy combined power generation and refrigeration device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20140723 Effective date of abandoning: 20160615 |
|
| AV01 | Patent right actively abandoned |
Granted publication date: 20140723 Effective date of abandoning: 20160615 |
|
| C25 | Abandonment of patent right or utility model to avoid double patenting |