CN106907204A - The absorption electricity-generating method of organic working medium and its system that a kind of low-temperature heat source drives - Google Patents

Abstract

The invention discloses a low-temperature heat source-driven organic working fluid absorption power generation method and its system, comprising the following steps: 1) heating the organic working medium to a saturated solution and passing it into the first vortex tube, expanding and dropping the organic working medium through the first vortex tube; After being compressed, a gas-liquid two-phase mixture is generated, 2) the first superheated steam flowing out from the first vortex tube is mixed with the first saturated steam and enters the first expander to expand and perform work; 3) the first superheated steam flowing out from the second vortex tube Under the action of gravity, the second solution flows through the recuperating evaporator to release heat and then enters the absorber; the first expander and the second expander work to drive the generator connected to it through the coupling to generate electricity. The invention separates the high-pressure saturated concentrated solution in two stages to generate refrigerant vapor for expansion and power generation. At the same time, a circulating pump is used to adjust the pressure of the system absorption process to reduce the heat load of the condenser, thereby improving the thermal efficiency of the power generation system. It has high technical economy.

Description

A low-temperature heat source-driven organic working fluid absorption power generation method and system thereof

Technical field:

The invention belongs to the technical field of low-grade heat energy utilization, and in particular relates to an organic working fluid absorption power generation method driven by a low-temperature heat source and a system thereof.

Background technique:

Absorption power generation technology is an effective way to utilize low-grade heat energy. At present, most of the absorption power generation systems use NH ₃ /H ₂ O solution as the working medium, such as the Kalina cycle system (a non-cooperative system of water and ammonia proposed by A. Kalina in 1989). The thermal cycle with boiling mixed liquid as the working medium), in the waste heat boiler type gas-steam combined cycle, using it to replace the Rankine cycle with water as the working medium can improve the single unit power and power supply efficiency of the combined cycle. However, the shortcomings of the Kalina circulatory system are quite obvious: _NH3 is poisonous and can easily cause harm to the human body; the operating pressure of the system is high, resulting in huge system equipment, and _NH3 is easy to leak. Once the _NH3 content in the air is between When it is 15-28% vol, it will explode when exposed to an open flame, which is not conducive to safe operation; the NH ₃ /H ₂ O absorption power generation system has relatively high requirements on the temperature of the driving heat source, which is not conducive to the development and utilization of low-grade energy. In addition, the existing absorption power generation system usually uses a refrigerant-poor solution (hereinafter referred to as "dilute solution", and the corresponding refrigerant-rich solution is referred to as "concentrated solution") on the low pressure (condensing pressure) side to absorb the exhaust gas of the expander, such as Invention patent ZL200910193870.4, the sensible heat of the dilute solution and the heat generated during the absorption process are taken away by the cooling medium, resulting in a certain amount of energy waste, resulting in low thermal efficiency of the system, and the conventional absorption system must be equipped with a throttling device in order to balance the pressure. This also increases the irreversible losses of the power generation system. On the other hand, the generator outlet of the conventional absorption power generation system is in a gas-liquid two-phase flow state, and the operation control is relatively complicated.

Therefore, the prior art needs to be improved and developed.

Invention content:

The purpose of the present invention is to provide a low-temperature heat source-driven organic working fluid absorption power generation method and its system, which can be adjusted according to the temperature of the heat source and the concentration of the solution for different application sites, and the circulation flow rate of the solution and the operating pressure of the absorption process. And by using the organic working medium mixture as the circulating working medium, the power generation system can operate at a lower temperature (≥70°C) and has higher thermal performance.

The first object of the present invention is to provide a kind of low-temperature heat source driven organic working fluid absorption power generation method, comprising the following steps:

1) Heat the organic working medium into a saturated solution and pass it into the first vortex tube. After the first vortex tube is expanded and depressurized, the organic working medium with a low boiling point is vaporized to form a gas-liquid two-phase mixture, and the first superheated steam is separated , the first saturated steam and the first solution;

2) The first superheated steam flowing out of the first vortex tube is mixed with the first saturated steam and enters the first expander for expansion; the first solution flowing out of the first vortex tube enters the second vortex tube under the action of gravity , through the second vortex tube expansion and depressurization, the low-boiling organic working medium is further vaporized to generate a gas-liquid two-phase mixture, and the second superheated steam, the second saturated steam and the second solution are separated, and the second vortex tube flows out The second superheated steam is mixed with the second saturated steam and enters the second expander to expand and perform work;

3) The second solution flowing out of the second vortex tube flows through the regenerating evaporator to release heat under the action of gravity and then enters the absorber; the first expander and the second expander work to drive the generator connected to it through the coupling Power generation by operation; the mixed steam of the first superheated steam and the first saturated steam in the first expander expands to the inlet pressure of the second expander and enters the absorber to be absorbed by the second solution from the second vortex tube; the second expander The mixed steam of the second superheated steam and the second saturated steam expands to the condensation pressure and then enters the condenser, and the mixed steam is cooled into a liquid state by the cooling medium outside the condenser;

4) The third solution cooled to a liquid state by the condenser is boosted to a certain pressure by the refrigerant pump, then flows through the preheater to absorb part of the heat, and then enters the absorber, where the third solution is absorbed by the heat generated during the process After being heated to the saturated liquid state under the corresponding pressure, it flows into the recuperation evaporator to be further heated to generate saturated steam; the fourth solution absorbed in the absorber flows through the preheater under the pressure boost of the first solution pump, After part of the heat is released in the preheater, it becomes a supercooled solution and then enters the jet adiabatic absorber as a working fluid, expands in the jet adiabatic absorber to form a low pressure or vacuum, and the steam generated in the connected regenerative evaporator is absorbed Inhalation, the working fluid and saturated steam are fully mixed in the jet adiabatic absorber to finally form a solution with a medium pressure, and then enter the heater after the second solution pump boosts the pressure to form a system cycle.

In the low-temperature heat source-driven organic working fluid absorption power generation method proposed by the present invention, the separation and steam generation process of the saturated solution at the outlet of the heater is carried out in two stages, the first stage separation and steam generation process is carried out in the first vortex tube, and the second stage separation The steam production process is carried out in the second vortex tube. The vortex tube adopts a counter-current vortex tube. Using its energy separation effect, after the high-pressure saturated concentrated solution enters from the inlet of the vortex tube, it expands and depressurizes, and part of the refrigerant is vaporized to produce a gas-liquid two-phase mixture, which rotates at a high speed and separates Saturated dilute solution, superheated refrigerant vapor and saturated refrigerant vapor flow out, the dilute solution flows out from the liquid outlet at the bottom of the vortex tube, and the superheated refrigerant vapor and saturated refrigerant vapor flow out from the hot gas outlet and cold air outlet of the vortex tube respectively.

The absorption process is carried out in two stages under intermediate pressure conditions, the first stage absorption process is carried out in the absorber, and the second stage absorption process is carried out in the jet adiabatic absorber. The absorber can adopt horizontal tube falling film absorber, vertical tube falling film absorber or bubbling absorber. The refrigerant liquid from the preheater enters the absorber through the tube side and is heated to saturation by the heat generated during the absorption process. liquid state. The jet adiabatic absorber adopts a gas-liquid two-phase flow ejector. The high-pressure subcooled dilute solution enters the ejector as the working fluid, and expands rapidly in it to form a low pressure or vacuum. The refrigerant vapor is inhaled, the dilute solution and the refrigerant vapor are fully mixed in the ejector and accompanied by the exchange of momentum and energy, and finally a concentrated solution with a medium pressure flows out from the outlet of the mixed fluid; the ejector has no heat exchange with the outside during the entire absorption process. In addition, the ejection effect produced in the jet adiabatic absorber also helps to promote the heat absorption and vaporization of the refrigerant liquid in the regenerative evaporator.

In the present invention, the vortex tube is used to replace the flash evaporator, and the energy separation effect of the vortex tube is used to separate the saturated concentrated solution of the high-pressure organic working medium in two stages. The pressure is adjusted, and the absorption is divided into two stages under the intermediate pressure condition, so as to realize the maximum recovery of the sensible heat and absorption heat of the dilute solution, reduce the heat load of the condenser, thereby improving the thermal efficiency of the power generation system, and has high technical economy.

The vortex tube is an energy separation device, which is composed of a nozzle, a vortex chamber, a separation orifice and a cold and hot two-end tube. During operation, the compressed gas expands in the nozzle, and then enters the vortex tube along the tangential direction at a high speed. When the airflow rotates at high speed in the vortex tube, it is separated into two parts of airflow with unequal total temperature after vortex transformation. The temperature of the airflow in the central part is low, while the temperature of the airflow in the outer part is high. Adjusting the ratio of cold and hot flows can get the best Good separation effect.

The organic working medium described in the step (1) includes low-boiling organic matter as a refrigerant and high-boiling organic matter as an absorbent, and the low-boiling organic matter is selected from R1234yf (2,3,3,3-tetrafluoropropene) , R1233zd(E) (trans-1-chloro-3,3,3-trifluoropropene), R1336mzz(Z) (cis-1,1,1,4,4,4-hexafluoro-2-butane One or more of R1234ze(E) (trans-1,3,3,3-tetrafluoropropene) and R1234ze(Z) (cis-1,3,3,3-tetrafluoropropene) The high-boiling point organic matter is selected from one of TrEGDME (triethylene glycol dimethyl ether), TEGDME (tetraethylene glycol dimethyl ether) and NMP (N-methylpyrrolidone).

In the present invention, one or more of the environmentally friendly organic compounds R1234yf, R1233zd(E), R1336mzz(Z), R1234ze(E) and R1234ze(Z) are used for the low-boiling point organic matter, and one or more of the high-boiling point organic matter is used One of TrEGDME, TEGDME and NMP. The boiling point difference between the low-boiling organic matter and the high-boiling organic matter is large, and the superheated steam and saturated steam at the outlets of the first vortex tube and the second vortex tube are mainly refrigerant steam.

Another object of the present invention is to propose a low-temperature heat source-driven organic working fluid absorption power generation system, including a heater for heating the organic working fluid into a saturated solution, a first vortex tube, a first expander, a second vortex tube, The second expander, generator, condenser, refrigerant pump, preheater, absorber, recuperator evaporator, first solution pump, jet adiabatic absorber and second solution pump, the saturated solution of the heater The outlet is connected to the second inlet of the first vortex tube, the first hot gas outlet of the first vortex tube is connected in parallel with the first cold air outlet and then connected to the third inlet of the first expander, and the first vortex tube The first liquid outlet is connected to the fourth inlet of the second vortex tube, and the second hot gas outlet of the second vortex tube is connected to the fifth inlet of the second expander after being connected in parallel with the second cold gas outlet. The second liquid outlet of the vortex tube is connected to the dilute solution inlet of the absorber after passing through the recuperation evaporator, the first outlet of the first expander is connected to the refrigerant vapor inlet of the absorber, and the second expander The second outlet of the absorber passes through the condenser, the refrigerant pump, the preheater, the absorber, and the heat recovery evaporator in turn, and then connects to the injection fluid inlet of the jet adiabatic absorber; the concentrated solution outlet of the absorber passes through the first The solution pump and the preheater are connected to the working fluid inlet of the jet adiabatic absorber, the mixed fluid outlet of the jet adiabatic absorber is connected to the first inlet of the heater after passing through the second solution pump, and the first expansion The first expander and the second expander are connected to the generator through a coupling.

In the present invention, the absorber can adopt a horizontal tube falling film absorber, a vertical tube falling film absorber or a bubble absorber, and the refrigerant liquid from the preheater enters the absorber through the tube and is absorbed. heat to a saturated liquid state. The jet adiabatic absorber adopts a gas-liquid two-phase flow ejector. The high-pressure subcooled dilute solution enters the ejector as the working fluid, and expands rapidly in it to form a low pressure or vacuum. The refrigerant vapor is inhaled, the dilute solution and the refrigerant vapor are fully mixed in the ejector and accompanied by the exchange of momentum and energy, and finally a concentrated solution with a medium pressure flows out from the outlet of the mixed fluid; the ejector has no heat exchange with the outside during the entire absorption process. In addition, the ejection effect produced in the jet adiabatic absorber also helps to promote the heat absorption and vaporization of the refrigerant liquid in the regenerative evaporator.

In the present invention, the refrigerant pump, the first solution pump and the second solution pump may use canned pumps or magnetic pumps. The generator can be a synchronous generator or an asynchronous generator. The connection between the various components of the system is metal pipe connection.

Preferably, the organic working medium includes low-boiling organic matter as a refrigerant and high-boiling organic matter as an absorbent, and the low-boiling organic matter is selected from R1234yf, R1233zd(E), R1336mzz(Z), R1234ze(E) and one or more of R1234ze(Z), the high-boiling organic matter is selected from one of TrEGDME, TEGDME and NMP, wherein the mass ratio of the low-boiling organic matter to the high-boiling organic matter is about 0.3-0.7.

Preferably, the position of the fourth inlet of the second vortex tube is lower than the position of the first liquid outlet of the first vortex tube, and the position of the second solution inlet of the regenerative evaporator is lower than that of the second vortex tube The position of the second liquid outlet, the position of the dilute solution inlet of the absorber is lower than the position of the second solution outlet of the regenerative evaporator. The position of the fourth inlet of the second vortex tube is lower than the position of the first liquid outlet of the first vortex tube, so as to ensure that the dilute solution at the outlet of the first vortex tube can flow into the second vortex tube by itself under the action of gravity; the regenerative evaporator The position of the second solution inlet of the second vortex tube is lower than the second liquid outlet of the second vortex tube, so as to ensure that the dilute solution at the outlet of the second vortex tube can flow into the reheating evaporator by itself under the action of gravity; the dilute solution inlet of the absorber The position is lower than the position of the second solution outlet of the regenerative evaporator to ensure that the dilute solution at the outlet of the regenerative evaporator can flow into the absorber by itself under the action of gravity.

Preferably, the heater, condenser, preheater and heat recovery evaporator are selected from one of shell and tube heat exchangers, falling film heat exchangers and plate heat exchangers.

Preferably, the first vortex tube is a reverse flow vortex tube, and the second vortex tube is a reverse flow vortex tube.

The first expander and the second expander may be screw expanders, scroll expanders or turbo expanders, or other types of expanders.

The beneficial effects of the present invention are:

1. The system uses an organic mixture as a circulating working medium. Compared with the conventional NH ₃ /H ₂ O solution, the temperature of the system-driven heat source can be reduced by about 20°C, which broadens the application range of the absorption power generation system;

2. The solution at the outlet of the heater is in a saturated liquid state, the heat absorption process of the solution does not involve a phase change process, the heat transfer coefficient is high, and the operation control is relatively simple;

3. The absorption process of the system is carried out under intermediate pressure conditions. The dilute solution does not enter the condenser, and all the heat contained in it is recovered, which effectively reduces the heat load of the condenser and increases the temperature of the solution at the inlet of the heater. Compared with the existing technology The thermal efficiency of the system can be increased by about 5-15%;

4. The system balances and adjusts the operating pressure of the absorption process through the combination of the two-stage expansion of the vortex tube and the circulating pump, and does not set a throttling device, which reduces the irreversible loss of the system.

Description of drawings:

Fig. 1 is the schematic structural view of the organic working fluid absorption power generation system driven by low-temperature heat source in Embodiment 1 of the present invention;

Reference signs: 100, heater; 101, first inlet; 101, saturated solution outlet; 200, first vortex tube; 201, second inlet; 202, first hot gas outlet; 203, first liquid outlet; 204, 300, the first expander; 301, the third inlet; 302, the first outlet; 400, the second vortex tube; 401, the fourth inlet; 402, the second hot gas outlet; 403, the second liquid outlet ;404, the second cold air outlet; 500, the second expander; 501, the fifth inlet; 502, the second outlet; 600, the generator; 700, the condenser; 701, the sixth inlet; 702, the third outlet; 800 , refrigerant pump; 801, seventh inlet; 802, fourth outlet; 900, preheater; 901, first refrigerant liquid inlet; 902, first refrigerant liquid outlet; 903, first solution inlet; 904, First solution outlet; 110, absorber; 111, second refrigerant liquid inlet; 112, refrigerant steam inlet; 113, dilute solution inlet; 114, second refrigerant liquid outlet; 115, concentrated solution outlet; 120, return Heat evaporator; 121, the third refrigerant liquid inlet; 122, the second solution outlet; 123, the second solution inlet; 124, refrigerant vapor outlet; 130, the first solution pump; 131, the eighth inlet; 132, the first Five outlets; 140, jet adiabatic absorber; 141, working fluid inlet; 142, injection fluid inlet; 143, mixed fluid outlet; 150, second solution pump; 151, ninth inlet; 152, sixth outlet.

detailed description:

The following examples are to further illustrate the present invention, rather than limit the present invention.

Unless otherwise specified, the experimental materials and reagents in the present invention are conventional commercially available products in the technical field. The arrows in Figure 1 indicate the direction of flow of vapor or liquid.

A low-temperature heat source-driven organic working fluid absorption power generation method, comprising the steps of:

1) Heat the organic working fluid into a saturated solution and pass it into the first vortex tube 200. After the first vortex tube 200 expands and depressurizes, the organic working medium with a low boiling point is vaporized to form a gas-liquid two-phase mixture, and the first vortex tube is separated. superheated steam, first saturated steam and first solution;

2) The first superheated steam flowing out from the first vortex tube 200 is mixed with the first saturated steam and enters the first expander 3 to expand and perform work; the first solution flowing out from the first vortex tube 200 enters the first solution under the action of gravity The second vortex tube 400 expands and depressurizes through the second vortex tube 400, and the organic working medium with a low boiling point is further vaporized to generate a gas-liquid two-phase mixture, and the second superheated steam, the second saturated steam and the second solution are separated, and the second superheated steam, the second saturated steam and the second solution are separated from the second The second superheated steam flowing out of the vortex tube 400 is mixed with the second saturated steam and enters the second expander 5 to expand and perform work;

3) The second solution flowing out of the second vortex tube 400 flows through the reheating evaporator 120 under the action of gravity and then enters the absorber 110; the first expander 300 and the second expander 500 work to drive it through the coupling The generator 600 connected to the generator operates to generate electricity; the mixed steam of the first superheated steam and the first saturated steam in the first expander 300 expands to the inlet pressure of the second expander 500 and then enters the absorber 110 and is taken from the second vortex tube 400 The second solution absorption; the mixed steam of the second superheated steam and the second saturated steam in the second expander 500 expands to the condensation pressure and enters the condenser 700, and the mixed steam is cooled into a liquid state by the cooling medium outside the condenser;

4) The third solution cooled to a liquid state by the condenser 700 is boosted to a certain pressure by the refrigerant pump 800, then flows through the preheater 900 to absorb part of the heat, and then enters the absorber 110, in which the third solution is The heat generated in the absorption process is heated to the saturated liquid state under the corresponding pressure and then flows into the recuperation evaporator 120 to be further heated to generate saturated steam; Next, it flows through the preheater 900, and after releasing part of the heat in the preheater 900, it becomes a supercooled solution and then enters the jet adiabatic absorber 140 as a working fluid, expands in the jet adiabatic absorber 140 to form a low pressure or vacuum, The steam generated in the connected recuperative evaporator 120 is sucked in, and the working fluid and saturated saturated steam are fully mixed in the jet adiabatic absorber 140 to finally form a solution with a medium pressure, and then enter the heating process after being boosted by the second solution pump 150 device 100 to form a system loop.

Example 1

The organic working fluid absorption power generation system driven by the low-temperature heat source as shown in Figure 1 includes a heater 100 for heating the organic working medium, a first vortex tube 200, a first expander 300, a second vortex tube 400, a second expander 500 , generator 600 , condenser 700 , refrigerant pump 800 , preheater 900 , absorber 110 , regenerative evaporator 120 , first solution pump 130 , jet adiabatic absorber 140 and second solution pump 150 . The saturated solution outlet 102 of the heater 100 is connected to the second inlet 201 of the first vortex tube 200, and the first hot gas outlet 202 of the first vortex tube 200 is connected in parallel with the first cold air outlet 204 to the third inlet of the first expander 300 301 connection, the first liquid outlet 203 of the first vortex tube 200 is connected with the fourth inlet 401 of the second vortex tube 400, the second hot gas outlet 402 of the second vortex tube 400 is connected in parallel with the second cold air outlet 404 and then connected with the second expansion The fifth inlet 501 of the machine 500 is connected, the second liquid outlet 403 of the second vortex tube 400 is connected with the second solution inlet 123 of the heat recovery evaporator 120, the second solution outlet 122 of the heat recovery evaporator 120 is connected with the absorber 110 The dilute solution inlet 113 is connected, the first outlet 302 of the first expander 300 is connected with the refrigerant vapor inlet 112 of the absorber 110, the second outlet 502 of the second expander 500 is connected with the sixth inlet 701 of the condenser 700, and condensed The third outlet 702 of the device 700 is connected to the seventh inlet 801 of the refrigerant pump 800, the fourth outlet 802 of the refrigerant pump 800 is connected to the first refrigerant liquid inlet 901 of the preheater 900, and the first inlet 901 of the preheater 900 The refrigerant liquid outlet 902 is connected with the second refrigerant liquid inlet 111 of the absorber 110, and the second refrigerant liquid outlet 114 of the absorber 110 is connected with the third refrigerant liquid inlet 121 of the heat recovery evaporator 120, and the heat recovery evaporator The refrigerant vapor outlet 124 of 120 is connected with the injection fluid inlet 142 of the jet adiabatic absorber 140, the concentrated solution outlet 115 of the absorber 110 is connected with the eighth inlet 131 of the first solution pump 130, and the fifth inlet 131 of the first solution pump 130 The outlet 132 is connected with the first solution inlet 903 of the preheater 900, the first solution outlet 904 of the preheater 900 is connected with the working fluid inlet 141 of the jet adiabatic absorber 140, and the mixed fluid outlet 143 of the jet adiabatic absorber 140 is connected with the second The ninth inlet 151 of the solution pump 150 is connected, the sixth outlet 152 of the second solution pump 150 is connected with the first inlet 101 of the heater 100, and the first expander 300 is connected to the second expander 500 and the generator 600 through a coupling. connected.

The connection between the various components of the system is metal pipe connection. The position of the fourth inlet 401 of the second vortex tube 400 is lower than the position of the first liquid outlet 203 of the first vortex tube 200, and the position of the second solution inlet 123 of the regenerative evaporator 120 is lower than the position of the first liquid outlet 203 of the second vortex tube 400. The position of the second liquid outlet 403 , the position of the dilute solution inlet 113 of the absorber 110 is lower than the position of the second solution outlet 122 of the regenerative evaporator 120 . The position of the fourth inlet 401 of the second vortex tube 400 is lower than the position of the first liquid outlet 203 of the first vortex tube 200, to ensure that the dilute solution at the outlet of the first vortex tube 200 can flow into the second vortex tube by itself under the action of gravity 400; the position of the second solution inlet 123 of the regenerative evaporator 120 is lower than the position of the second liquid outlet 403 of the second vortex tube 400, so as to ensure that the dilute solution at the outlet of the second vortex tube 400 can flow in by itself under the action of gravity Reheating evaporator 120; the position of the dilute solution inlet 113 of the absorber 110 is lower than the position of the second solution outlet 122 of the regenerating evaporator 120, so as to ensure that the dilute solution at the outlet of the regenerating evaporator 120 can move by itself under the action of gravity into the absorber 110.

The working fluid of the system can be one or more of R1234yf, R1233zd(E), R1336mzz(Z), R1234ze(E) or R1234ze(Z) as the refrigerant and one of the high boiling organic compounds TrEGDME, TEGDME or NMP As a mixture of absorbents. When actually selecting the working fluid, one or more of R1234yf, R1233zd(E), R1336mzz(Z), R1234ze(E) or R1234ze(Z) can be selected to be mixed with one of TrEGDME, TEGDME or NMP for power generation The working fluid of the system can be selected by those skilled in the art according to actual needs. In this embodiment, the R1233zd(E)/TEGDME solution is used as the working fluid, wherein the mass ratio of R1233zd(E) to TEGDME is 0.3-0.7. Compared with the existing Technology, in this embodiment, the temperature of the driving heat source of the power generation system can be reduced by about 20°C, which broadens the application range of the absorption power generation system. This implementation uses a low-grade heat source of about 90°C, and the thermal efficiency of the power generation system can be increased by about 5% to 15%. %.

Using R1233zd(E)/TEGDME solution as the circulating working medium, the working principle of the organic working medium absorption power generation system driven by low temperature heat source is as follows:

The supercooled R1233zd(E)/TEGDME basic (concentrated) solution is heated to a saturated solution by an external low-grade heat source in the heater 100, and then enters the first vortex tube 200, and is expanded and depressurized by the first vortex tube 200, with a low boiling point The organic working medium R1233zd (E) is vaporized to form a gas-liquid two-phase mixture, which undergoes high-speed rotating flow in the first vortex tube 200 to separate superheated gas, saturated gas and saturated solution, and the R1233zd flowing out of the first vortex tube 200 (E) Superheated steam and saturated steam are mixed into the first expander 300 to expand and perform work; the R1233zd(E)/TEGDME dilute solution flowing out from the first vortex tube 200 enters the second vortex tube 400 under the action of gravity, and passes through the second vortex tube 400 again. Expansion and decompression, the low boiling point organic working medium R1233zd (E) is vaporized to generate a gas-liquid two-phase mixture, in which the superheated gas, saturated gas and saturated solution are separated through high-speed rotating flow, and the water flowing out from the second vortex tube 400 R1233zd(E) superheated steam and saturated steam are mixed into the second expander 500 to expand and perform work; the R1233zd(E)/TEGDME dilute solution flowing out of the second vortex tube 400 flows through the reheating evaporator 120 under the action of gravity to release heat Then enter the absorber 110; the first expander 300 and the second expander 500 work to drive the generator 600 connected to the first expander 300 and the second expander 500 through a coupling to run and generate electricity; the first expander 300 After the R1233zd(E) steam expands to the inlet pressure of the second expander 500, it enters the absorber 110 and is absorbed by the R1233zd(E)/TEGDME dilute solution from the second vortex tube 400; the R1233zd(E) in the second expander 500 The steam expands to the condensation pressure and enters the condenser 700, where it is cooled to a liquid state by the external cooling medium of the condenser; the R1233zd(E) refrigerant liquid is boosted to a certain pressure by the refrigerant pump 800 and then flows through the preheater 900 absorbs part of the heat, and then enters the absorber 110, where it is heated to a saturated liquid state under the corresponding pressure by the heat generated during the absorption process, and then flows into the regenerative evaporator 120, where it is further heated to generate R1233zd(E) saturated steam; the R1233zd(E)/TEGDME solution that has been absorbed in the absorber 110 flows through the preheater 900 under the pressure boost of the first solution pump 130, and is released by reverse flow in the preheater 900 Part of the heat turns into a supercooled solution and enters the jet adiabatic absorber 140 as a working fluid, where it expands rapidly to form a low pressure or vacuum, and the R1233zd(E) refrigerant vapor generated in the regenerative evaporator 120 connected to it is sucked in, The dilute solution and the refrigerant vapor are fully mixed in the jet adiabatic absorber 140 and accompanied by the exchange of momentum and energy, finally forming a basic solution of R1233zd(E)/TEGDME at an intermediate pressure, which is then boosted by the second solution pump 150 and then enters the heating system. The heater 100 forms a system circulation.

The low-temperature heat source-driven organic working fluid absorption power generation method and system thereof provided by the present invention have been described above in detail. The descriptions of the above embodiments are only used to help understand the technical solutions and core ideas of the present invention. It should be pointed out that for this invention For those skilled in the art, without departing from the principles of the present invention, some improvements and modifications can be made to the present invention, and these improvements and modifications also fall within the protection scope of the claims of the present invention.

Claims (7)

1. A low-temperature heat source-driven organic working fluid absorption method for generating electricity, is characterized in that, comprises the steps: 1) Heat the organic working fluid into a saturated solution and pass it into the first vortex tube (200), after the first vortex tube (200) expands and depressurizes, the organic working medium with a low boiling point is vaporized to form a gas-liquid two-phase mixture, separating the first superheated steam, the first saturated steam and the first solution; 2) The first superheated steam flowing out from the first vortex tube (200) is mixed with the first saturated steam and enters the first expander (300) to expand and perform work; the first solution flowing out from the first vortex tube (200) is Under the action of gravity, it enters the second vortex tube (400), expands and depressurizes through the second vortex tube (400), and the organic working medium with low boiling point is further vaporized to form a gas-liquid two-phase mixture, and the second superheated steam, the second Saturated steam and the second solution, the second superheated steam flowing out from the second vortex tube (400) is mixed with the second saturated steam and enters the second expander (500) to expand and perform work; 3) The second solution flowing out of the second vortex tube (400) flows through the reheating evaporator (120) under the action of gravity and then enters the absorber (110); the first expander (300) and the second expander The machine (500) works to drive the generator (600) connected to it through the shaft coupling to run and generate electricity; the mixed steam of the first superheated steam and the first saturated steam in the first expander (300) expands to the second expander (500 ) enters the absorber (110) and is absorbed by the second solution from the second vortex tube (400); the mixed steam of the second superheated steam and the second saturated steam in the second expander (500) expands to condensate Enter the condenser (700) after the pressure, and the mixed steam is cooled into a liquid state by the cooling medium outside the condenser; 4) The third solution cooled to a liquid state by the condenser (700) is boosted to a certain pressure by the refrigerant pump (800), then flows through the preheater (900) to absorb part of the heat, and then enters the absorber (110), where The third solution in the absorber (110) is heated to the saturated liquid state under the corresponding pressure by the heat generated during the absorption process, and then flows into the recuperation evaporator (120) to be further heated to generate saturated steam; the absorber (110) absorbs The finished fourth solution flows through the preheater (900) under the pressure boost of the first solution pump (130), and after releasing part of the heat in the preheater (900), it becomes a supercooled solution as a working solution. The fluid enters the jet adiabatic absorber (140), and expands in the jet adiabatic absorber (140) to form a low pressure or vacuum, and the steam generated in the connected regenerative evaporator (120) is sucked in, and the working fluid and saturated steam are jetted Fully mixed in the adiabatic absorber (140), finally forming a solution with a middle pressure, and then entering the heater (100) after being boosted by the second solution pump (150), forming a system circulation. 2. The organic working medium absorption power generation method driven by low temperature heat source according to claim 1, characterized in that: the organic working medium described in step (1) comprises low-boiling point organic matter as refrigerant and high-temperature organic working medium as absorbent Boiling point organic matter, described low boiling point organic matter is selected from one or more of R1234yf, R1233zd (E), R1336mzz (Z), R1234ze (E) and R1234ze (Z), and described high boiling point organic matter is selected from TrEGDME, One of TEGDME and NMP. 3. An organic working fluid absorption power generation system driven by a low-temperature heat source, characterized in that it includes a heater (100) that heats the organic working fluid into a saturated solution, a first vortex tube (200), a first expander (300 ), the second vortex tube (400), the second expander (500), the generator (600), the condenser (700), the refrigerant pump (800), the preheater (900), the absorber (110), regenerative evaporator (120), first solution pump (130), jet adiabatic absorber (140) and second solution pump (150), the saturated solution outlet (102) of the heater (100) is connected to the first The second inlet (201) of the vortex tube (200) is connected, and the first hot gas outlet (202) of the first vortex tube is connected in parallel with the first cold air outlet (204) and then connected to the first expansion machine (300). Three inlets (301), the first liquid outlet (203) of the first vortex tube (200) is connected with the fourth inlet (401) of the second vortex tube (400), and the second vortex tube (400) ) of the second hot gas outlet (402) and the second cold gas outlet (404) are connected in parallel to the fifth inlet (501) of the second expander (500), and the second liquid of the second vortex tube (400) The outlet (403) is connected to the dilute solution inlet (113) of the absorber (110) after passing through the recuperating evaporator (120), and the first outlet (302) of the first expander (300) is connected to the absorber (110) ) is connected to the refrigerant steam inlet (112), and the second outlet (502) of the second expander (500) passes through the condenser (700), refrigerant pump (800), preheater (900), The absorber (110) and the regenerative evaporator (120) are connected to the injection fluid inlet (142) of the jet adiabatic absorber (140); the concentrated solution outlet (115) of the absorber (110) passes through the first A solution pump (130) and a preheater (900) are connected to the working fluid inlet (131) of the jet adiabatic absorber (140), and the mixed fluid outlet (143) of the jet adiabatic absorber (140) passes through the first The second solution pump (150) is connected to the first inlet (101) of the heater (100), the first expander (300) and the second expander (500) are connected to the generator (600) through a coupling connected. 4. The low-temperature heat source-driven organic working fluid absorption power generation system according to claim 3, characterized in that: said organic working medium comprises low-boiling point organic matter as refrigerant and high-boiling point organic matter as absorbent, said The low-boiling organic matter is selected from one or more of R1234yf, R1233zd (E), R1336mzz (Z), R1234ze (E) and R1234ze (Z), and the high-boiling organic matter is selected from TrEGDME, TEGDME and NMP A sort of. 5. The low-temperature heat source-driven organic working fluid absorption power generation system according to claim 3, characterized in that: the position of the fourth inlet (401) of the second vortex tube (400) is lower than that of the first vortex tube The position of the first liquid outlet (203) of (200), the position of the second solution inlet (123) of the described regenerative evaporator (120) is lower than the second liquid outlet (403) of the second vortex tube (400). ), the position of the dilute solution inlet (113) of the absorber (110) is lower than the position of the second solution outlet (122) of the regenerative evaporator (120). 6. The organic working fluid absorption power generation system driven by a low-temperature heat source according to claim 3 or 4, characterized in that: said heater (100), condenser (700), preheater (900) and return The heat evaporator (120) is selected from one of shell and tube heat exchangers, falling film heat exchangers and plate heat exchangers. 7. The organic working fluid absorption power generation system driven by a low-temperature heat source according to claim 3 or 4, characterized in that: the first vortex tube (200) is a countercurrent vortex tube, and the second vortex tube (400) is a countercurrent type vortex tube.