CN112797317B - A supercritical carbon dioxide cycle generator set working fluid recovery system and control method - Google Patents
A supercritical carbon dioxide cycle generator set working fluid recovery system and control method Download PDFInfo
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- CN112797317B CN112797317B CN202110116060.XA CN202110116060A CN112797317B CN 112797317 B CN112797317 B CN 112797317B CN 202110116060 A CN202110116060 A CN 202110116060A CN 112797317 B CN112797317 B CN 112797317B
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D1/00—Pipe-line systems
- F17D1/02—Pipe-line systems for gases or vapours
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01D—NON-POSITIVE DISPLACEMENT MACHINES OR ENGINES, e.g. STEAM TURBINES
- F01D15/00—Adaptations of machines or engines for special use; Combinations of engines with devices driven thereby
- F01D15/10—Adaptations for driving, or combinations with, electric generators
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
- F01K25/08—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours
- F01K25/10—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours the vapours being cold, e.g. ammonia, carbon dioxide, ether
- F01K25/103—Carbon dioxide
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K7/00—Steam engine plants characterised by the use of specific types of engine; Plants or engines characterised by their use of special steam systems, cycles or processes; Control means specially adapted for such systems, cycles or processes; Use of withdrawn or exhaust steam for feed-water heating
- F01K7/32—Steam engine plants characterised by the use of specific types of engine; Plants or engines characterised by their use of special steam systems, cycles or processes; Control means specially adapted for such systems, cycles or processes; Use of withdrawn or exhaust steam for feed-water heating the engines using steam of critical or overcritical pressure
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D1/00—Pipe-line systems
- F17D1/08—Pipe-line systems for liquids or viscous products
- F17D1/14—Conveying liquids or viscous products by pumping
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D3/00—Arrangements for supervising or controlling working operations
- F17D3/01—Arrangements for supervising or controlling working operations for controlling, signalling, or supervising the conveyance of a product
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Abstract
一种超临界二氧化碳循环发电机组工质回收系统及控制方法，包括液态储罐，来自液态储罐的CO2工质通过低温活塞式加压泵A增压后进入蒸发器，蒸发器水侧配置有一个循环水泵；CO2工质经过蒸发器加热气化后依次进入缓冲罐、稳压罐，稳压罐输出端接入高压储罐，高压储罐的出口跟电热油加热器相连，电热油加热器输出端通过压缩机干气密封管线连接压缩机，通过供透平机干气密封管线连接透平机，压缩机通过压缩机排气管线连接回收罐A，透平机通过透平机排气管线连接回收罐B，回收罐A和回收罐B输出端汇合后连接液态储罐。本发明能够实现S‑CO2循环发电机组在启动及运行过程中近零排放，降低了因CO2气体排放造成的经济损失，有效防范了现场作业的安全风险。
A supercritical carbon dioxide circulating power generation unit working medium recovery system and control method, including a liquid storage tank, CO2 working medium from the liquid storage tank is pressurized by a low-temperature piston booster pump A and then enters an evaporator, and a circulating water pump is configured on the water side of the evaporator; CO2 working medium is heated and gasified by the evaporator and then enters a buffer tank and a pressure regulating tank in sequence, the output end of the pressure regulating tank is connected to a high-pressure storage tank, the outlet of the high-pressure storage tank is connected to an electric oil heater, the output end of the electric oil heater is connected to the compressor through a compressor dry gas sealing pipeline, and is connected to the turbine through a turbine dry gas sealing pipeline, the compressor is connected to a recovery tank A through a compressor exhaust pipeline, the turbine is connected to a recovery tank B through a turbine exhaust pipeline, and the output ends of the recovery tanks A and B are connected to a liquid storage tank after merging. The present invention can achieve near-zero emissions of the S- CO2 circulating power generation unit during startup and operation, reduce the economic losses caused by CO2 gas emissions, and effectively prevent safety risks in field operations.
Description
Technical Field
The invention relates to the technical field of supercritical carbon dioxide circulating generator sets, in particular to a working medium recovery system and a control method of a supercritical carbon dioxide circulating generator set.
Background
Supercritical carbon dioxide (S-CO 2 for short) is circulated and proposed in the 50-60S of the 20 th century. In the last 10 years, a large amount of manpower and material resources are invested in research of S-CO 2 circulation in many countries, so that the S-CO 2 circulation becomes an industry hotspot. On one hand, the development trend is related to the efficient and flexible utilization of various energy sources by human beings and the reduction of environmental pollution, and on the other hand, the development of Rankine cycle mainly taking water vapor as working medium is limited by factors such as metal materials and the like to enter a bottleneck period, and CO 2 is favored as a non-toxic, colorless and odorless working medium which is nonflammable and is very easy to obtain in nature.
Unlike conventional thermal power generating unit, the S-CO 2 circulating generator set is equipped with a complete liquefied storage tank, a booster pump, an evaporator, a buffer tank, a pressure stabilizing tank, a high-pressure storage tank and auxiliary equipment which take CO 2 as working medium, and the series of equipment forms a storage, charging and discharging and monitoring system of the whole CO 2 working medium, so that stable, reliable and CO 2 working medium meeting technological system requirement parameters is provided for the S-CO 2 circulating generator set. However, the existing literature on the S-CO 2 cycle generator set can rarely see a CO 2 working medium recovery device.
The S-CO 2 circulating generator set core equipment comprises a main compressor, a high-low pressure turbine and auxiliary equipment thereof. Unlike conventional thermal power generating units, the main compressor shaft end seal adopts CO 2 gas as sealing gas, and the high-pressure and low-pressure turbine shaft end seal also adopts CO 2 gas as sealing gas, similar to the shaft seal steam of a turbine of the thermal power generating unit. Before the compressor or turbine is started, CO 2 gas with specific temperature and pressure is required to be filled, and the gas is called dry gas sealing gas. In order to quickly meet the temperature of the dry gas seal gas in the initial stage of starting, besides the dry gas seal electric heating oil heating device, a large amount of exhaust is needed to be carried out through a compressor cylinder body and a pipeline in actual operation to raise the temperature of the dry gas seal gas, so that a large amount of CO 2 gas is wasted. In addition, when various storage tanks filled with CO 2 gas are overhauled or the system pressure is over-limited, a large amount of CO 2 is required to be discharged, so that the waste of system working media is increased. The emission of large amounts of CO 2 gas directly causes objective economic losses on the one hand, and on the other hand, the accumulation of CO 2 gas in small spaces causes great safety risks and at the same time environmental greenhouse gas pollution.
Disclosure of Invention
In order to overcome the defects in the prior art, the invention aims to provide a working medium recovery system of a supercritical carbon dioxide cycle generator set and a control method, wherein the system integrates a CO 2 working medium recovery system on the basis of storage, charging and discharging and monitoring of a CO 2 working medium, so that a complete flow is formed. The novel CO 2 working medium recovery system comprises different functional units such as collection, pressurization, cooling liquefaction, pollution discharge, transportation and the like, can realize near zero emission of the S-CO 2 circulating generator set in the starting and running processes, remarkably reduces economic loss caused by CO 2 gas emission, and effectively prevents the safety risk of on-site operation.
In order to achieve the above purpose, the technical scheme adopted by the invention is as follows:
A working medium recovery system of a supercritical carbon dioxide circulating generator set comprises a liquid storage tank 1, wherein a CO 2 working medium from the liquid storage tank 1 enters an evaporator 3 after being pressurized by a low-temperature piston type booster pump A2, a circulating water pump 4 is arranged on the water side of the evaporator 3, the CO 2 working medium sequentially enters a buffer tank 5 and a pressure stabilizing tank 6 after being heated and gasified by the evaporator 3, a branch is led out of the pressure stabilizing tank 6 to be connected to a high-pressure storage tank 7, an outlet of the high-pressure storage tank 7 is connected with an electric heating oil heater H, an output end of the electric heating oil heater H is connected with a compressor 8 through a compressor dry gas sealing pipeline I, the compressor 8 is connected with a turbine 9 through a turbine air supply pipeline II, the compressor 8 is connected with a recovery tank A10 through a compressor exhaust pipeline III, the turbine 9 is connected with a recovery tank B11 through a turbine exhaust pipeline II IV, and the output ends of the recovery tank A10 and the recovery tank B11 are converged and then connected with the liquid storage tank 1.
And cylinder exhaust, pipeline exhaust and dry gas sealing leakage of the compressor 8 are summarized to a compressor exhaust pipeline III.
And the carbon ring protection gas, cylinder exhaust gas and dry gas sealing leakage of the turbine 9 are summarized to a turbine exhaust pipeline II IV.
The input end of the turbine exhaust pipeline II IV is connected with an exhaust pipeline III V, a pneumatic shutoff valve I31 and a check valve VI 27 are arranged on the exhaust pipeline III V, and the exhaust pipeline III V is communicated with the system exhaust pipeline to supply air and overhaul and exhaust from each storage tank.
And a normally-closed pneumatic shutoff valve six 37 for isolation is arranged between the exhaust pipeline I III and the exhaust pipeline II IV.
The recovery tank A10 and the recovery tank B11 have the same structure, the recovery tank A10 is provided with a first vacuum pump 16, a first vacuum pump 16 and a second matched pneumatic shutoff valve 32 for vacuumizing the tank body before recovering working media, the recovery tank A10 is provided with a working media compression device and a first compression motor 20, the side surface of the recovery tank A is provided with a first working media cooling device 18, the recovery tank A10 is provided with a first sewage disposal tank 14, and a switch is controlled by a fourth pneumatic shutoff valve 34 at the bottom.
The recovery tank A10 and the working medium recovery inlet pipeline are sequentially provided with a check valve I22 and a regulating valve I28, and the check valve I and the regulating valve I are used for controlling the parameters of gas entering the recovery tank A.
The bottom of the recovery tank A10 is connected with the delivery pump B42, and the pressurized and liquefied working medium is re-delivered into the liquid storage tank 1 through the check valve III 24 and the regulating valve III 30.
And the outlet of the conveying pump B42 is provided with a pipeline in parallel, the pipeline is directly connected to the inlet of the evaporator 3 through the regulating valve IV 36 and the check valve V26, and when the gas pressure and the temperature in the recovery tank A10 meet the air inlet requirement of the evaporator, the pipeline is directly fed into the liquid storage tank 1 and does not enter the liquid storage tank 1.
A control method of a working medium recovery system of a supercritical carbon dioxide circulating generator set comprises the following steps:
Working medium recovery control of the exhaust side of the compressor 8:
The working medium recovery of the exhaust side of the compressor 8 is mainly carried out at the initial stage of starting and after stopping of the compressor 8, the CO 2 working medium in the high-pressure storage tank 7 is required to be introduced into an electric heating oil heater H for heating at the initial stage of starting of the compressor 8, the heated CO 2 working medium enters a compressor dry gas sealing disc station through an air supply pipeline I, a large amount of unheated cold CO 2 working medium in the air supply pipeline I is introduced into the compressor 8, the cold CO 2 working medium is exhausted through an exhaust valve 39 of a compressor cylinder body and an exhaust valve 38 of an outlet pipeline, and the exhausted part of gas is summarized into a compressor exhaust pipeline I and enters a recovery tank A through a check valve I22 and a regulating valve I28;
after the compressor 8 is stopped, according to normal stop protection logic, the compressor outlet pipeline blow-off valve 38 is opened in an interlocking way, and a large amount of high-temperature and high-pressure CO 2 working medium enters an exhaust pipeline III and finally enters a recovery tank A10;
Working medium recovery control of the exhaust side of the turbine 9:
The working medium recovery at the exhaust side of the turbine 9 is also carried out at the initial stage of turbine starting and after the turbine is stopped, the CO 2 working medium in the high-pressure storage tank 7 is introduced into the electric heating oil heater H for heating, the heated CO 2 working medium enters the turbine dry gas sealing disc station from the air supply pipeline II, a large amount of unheated low-temperature CO 2 working medium in the air supply pipeline II is introduced into the turbine 9, the low-temperature CO 2 working medium is discharged through the turbine carbonization protection discharge valve 40 and the cylinder body discharge valve 41, and the discharged part of gas is summarized to the turbine exhaust pipeline IV and enters the recovery tank B11 through the check valve II 23 and the regulating valve II 29;
The gas coming from the system vent pipeline and the overhauling exhaust gas from each storage tank are summarized to an exhaust pipeline III V, and are controlled by a pneumatic valve 31 and a check valve VI 27, so that the gas can enter a pressure stabilizing tank A or a pressure stabilizing tank B, and the gas is discharged according to the actual condition of the system;
control of recovery tank a 10:
before the recovery tank A10 recovers the working medium, firstly, opening a pneumatic shutoff valve II 32, starting a vacuum pump I16, vacuumizing the recovery tank A10, when a pressure meter P a in the recovery tank A10 displays more than 80kPa, characterizing that vacuumizing is completed, automatically closing the pneumatic shutoff valve II 32, interlocking the vacuum pump I16, completing the vacuumizing of the recovery tank A10, opening an air inlet regulating valve of the recovery tank A10, introducing the air in an exhaust pipeline I III into the recovery tank A10, monitoring the pressure P a in the tank body in real time, after the pressure P a reaches 4.5MPa, starting a compression motor 20 of the recovery tank A10, compressing the recovered working medium, simultaneously inputting a cooling device I18 of the recovery tank A10, cooling the compressed working medium to below 8 ℃ (the liquid phase point corresponding to CO 2 of 4.5MPa is below 9 ℃, monitoring the temperature of the working medium in real time, compressing and cooling the working medium to become liquid, starting a conveying pump B42, conveying the liquefied working medium to the whole storage tank 2, and completing the recovery of the whole working medium;
Before the recovery tank A10 is started for the first time, the recovery tank A10 is purged by using the introduced CO 2 working medium and is purged into the sewage disposal tank A14 through the pneumatic valve 34, the bottom of the recovery tank is opened for 1min every 8 hours to drain water and air, and when the liquid storage tank 1 breaks down or the pressure at the outlet of the delivery pump B42 is not matched with the pressure of the liquid storage tank 1, the liquid working medium in the recovery tank A10 is directly sent into the evaporator 3 through the regulating valve four 36;
The control method of the recovery tank B11 is similar to that of the recovery tank A10, the first compressor exhaust pipeline III and the second turbine exhaust pipeline IV are combined together by opening the pneumatic shutoff valve six 37 and are respectively sent into different recovery tanks according to actual needs, and when one tank body fails in actual use, the inlet air is cut off through the inlet regulating valve, and the other tank body is started to recover working media.
A pneumatic shutoff valve six 37 is arranged between the first compressor exhaust pipeline III and the second turbine exhaust pipeline IV, and the valve is a normally closed valve and is used for isolating exhaust of the pipelines.
The invention has the beneficial effects that:
1) On the basis of the storage, charging and discharging and monitoring of working media of a conventional S-CO 2 circulating power generation system, a CO 2 working media recovery system is integrated, and the whole complete flow is formed.
2) The CO 2 working medium recovery system comprises different functional units such as collection, pressurization, cooling liquefaction, pollution discharge and transportation, can realize near zero emission of the S-CO 2 circulating generator set in the starting and running processes, remarkably reduces economic loss caused by CO 2 gas emission, effectively prevents safety risks of on-site operation, and reduces greenhouse gas pollution.
3) The recovery system is provided with two rows of recovery tanks in parallel, so that the quantity of recovered working media is increased, and the recovery system has more flexibility in use. The method has the characteristics of fault removal, interactive operation, real-time monitoring of operation parameters and the like.
4) The vacuum pump arranged in the recovery tank can pump the tank body to vacuum above-80 kPa before the working medium is recovered, and when the vacuum reaches a set value, the vacuum pump is stopped in an interlocking way, and the inlet pneumatic valve is closed in an interlocking way, so that the purity of the recovered carbon dioxide is ensured.
5) The recovery tank is provided with a bottom sewage disposal tank, so that the recovery tank can be used for purging the tank body during the first recovery, and can be matched with the tank body to release pressure and drain water and dredge air at any time in the use process.
6) Automatic sewage draining, namely opening a drain valve for 1min every 8 hours at the bottom of the recovery tank to drain water and air at the bottom.
7) And after the purity in the recovery tank is monitored to be qualified, starting compression and cooling, and discharging preferentially when the purity is unqualified.
8) The temperature, pressure and purity monitoring device arranged on the recovery tank can realize real-time display in the whole recovery process and serve as a basis for equipment control.
Drawings
FIG. 1 is a schematic flow chart of the present invention.
In the figure, 1, a liquid storage tank; 2 a pressurizing pump, 3 a evaporator, 4a water pump, 5a buffer tank, 6a surge tank, 7a high-pressure storage tank, 8 a compressor, 9 a turbine, 10a recovery tank A, 11 a recovery tank B, 12 a low-temperature delivery pump B, 13 a low-temperature delivery pump C, 14a blow-down tank I, 15 a blow-down tank II, 16 a vacuum pump I17, a vacuum pump II, 18 a cooling device I, 19 a cooling device II, 20 a recovery tank compression motor I, 21 a recovery tank compression motor II, 22 a check valve I, 23 a check valve II, 24 a check valve III, 25 a check valve IV, 26 a check valve V, 27 a check valve VI, 28 a regulating valve I, 29 a regulating valve II, 30 a regulating valve III, 36 a regulating valve IV, 31 a pneumatic shutoff valve I, 32 a pneumatic shutoff valve II, 33 a pneumatic shutoff valve III, 34 a pneumatic shutoff valve IV, 35 a pneumatic shutoff valve V, 37 a pneumatic shutoff valve VI, 38 a pneumatic shutoff valve V, 38, a pneumatic shutoff valve V, a compressor cylinder body, a compressor inlet and a discharge valve B, a pneumatic shutoff valve V, a cylinder body, a compressor inlet and a discharge valve C, a cylinder body, a pneumatic shutoff valve B, a cylinder body, a compressor inlet, and a turbine inlet.
The device comprises an I air supply pipeline I, an II air supply pipeline II, an III air exhaust pipeline I, an IV air exhaust pipeline II, a V pipeline III, an H which is an electric heating oil heater, P a which is a pressure measuring point of a working medium in a pressure stabilizing tank A, T a which is a temperature measuring point of the working medium in the pressure stabilizing tank A, S a which is a purity measuring point of the working medium in the pressure stabilizing tank A, P b which is a pressure measuring point of the working medium in the pressure stabilizing tank B, T b which is a temperature measuring point of the working medium in the pressure stabilizing tank B, S b which is a purity measuring point of the working medium in the pressure stabilizing tank B, P 1 which is a pressure of a liquid storage tank, and P 2 which is an inlet pressure of an evaporator.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
In a conventional S-CO 2 cycle generator set, as shown in fig. 1, a CO 2 working medium from a liquid storage tank 1 is pressurized by a low-temperature piston type booster pump a and then enters an evaporator 3, a water bath type electric heater in the evaporator 3 is used for heating and gasifying, a circulating water pump 4 is arranged on the water side of the evaporator 3, the heated and gasified CO 2 working medium sequentially enters a buffer tank 5 and a pressure stabilizing tank 6, and the pressure stabilizing tank 6 is used as an air inlet circulation unit of the S-CO 2 cycle generator set, so that stable air inlet pressure needs to be maintained. A branch is led out from the pressure stabilizing tank 6 and connected to the high-pressure storage tank 7, the high-pressure storage tank 7 is connected with the electric heating oil heater H, and the temperature of gas entering the compressor and the turbine for sealing dry gas can be set through H. When the unit is started and stopped, the gas in the high-pressure storage tank 7 is heated to a set temperature by the electric heating oil heater H, and then is respectively supplied to the compressor 8 and the turbine 9 through the compressor dry gas sealing pipeline I and the turbine gas supply pipeline II, and one part of the dry gas sealing gas entering the compressor 8 is discharged through the leakage pipeline, and the other part of the dry gas sealing gas is directly discharged from the cylinder body exhaust and the outlet pipeline of the compressor 8 to meet the requirement of entering the gas temperature of the compressor, and is directly discharged to the atmosphere. Into the turbine 9. In addition, during the operation of the unit, the incoming air from the system vent pipeline and the exhaust air from the overhaul of each storage tank are directly discharged to the atmosphere.
In the invention, the vent line III of the compressor 8, the vent line IV of the turbine, the incoming gas from the system vent pipeline and the total vent line V from the overhaul of each storage tank are combined together to form a total vent line, and the total vent line is respectively introduced into the recovery tanks A10 and 11 and the recovery tank B. The recovered working medium is pressurized, cooled and liquefied in the recovery tank A/B, then is recovered and enters the liquid storage tank 1 through the delivery pump 12/13, the check valve III 24/25 and the regulating valve III 30, and the other part of the working medium enters the evaporator inlet through the regulating valve IV 36 and the check valve V26, so that the recovery of the whole working medium is completed.
Taking the recovery tank A10 as an example, the complete recovery device comprises a vacuum pump I16, a control valve 32, a tank body compressor 20, a sewage disposal tank I14, a control valve 34, a recovery tank cooling device I18, a delivery pump B for pressurizing and liquefying working medium to flow back, a temperature measuring point T a for monitoring parameters of the recovery tank in real time, a pressure measuring point P a, a purity measuring point S a, a check valve I22 for controlling working medium recovery and an inlet regulating valve I28.
The recovery tank B has the same structure.
The cylinder exhaust (controlled by the pneumatic valve 39), the outlet pipe exhaust (controlled by the pneumatic valve 38) and the dry gas seal leakage of the compressor 8 are summarized to a compressor exhaust pipeline III.
The carbocycle protection gas (controlled by the pneumatic valve 40), the cylinder exhaust gas (controlled by the pneumatic valve 41) and the dry gas seal leakage of the turbine 9 are summarized to a turbine exhaust line II.
And the air coming from the system emptying pipeline is collected from overhauling exhaust of each storage tank to an exhaust pipeline III V.
A normally closed isolation valve 37 is provided between the first and second exhaust lines III and IV for isolation.
The exhaust line III V is integrated into the exhaust line II IV through the pneumatic shutoff valve I31 and the check valve VI 27.
The recovery tank A is provided with a first vacuum pump 16 and a second matched pneumatic shutoff valve 32, and is used for vacuumizing the tank body before working medium recovery.
The recovery tank A is provided with a working medium compression device and is provided with a compression motor 20, and compression is started when the tank body pressure reaches a certain static pressure.
The recovery tank A is provided with a first working medium cooling device 18, and can reduce the temperature in the working medium compression process so as to compress, cool and liquefy the working medium.
The recovery tank A is provided with a first sewage draining tank 14, a switch is controlled by a fourth pneumatic shutoff valve 34 at the bottom, and system sewage draining is performed before the recovery tank is pressurized.
The bottom of the recovery tank A is connected with the delivery pump B, and the pressurized and liquefied working medium is re-delivered into the liquid storage tank 1 through the check valve III 24 and the regulating valve III 30.
And the outlet of the conveying pump B is provided with a pipeline in parallel, the pipeline is directly connected to the inlet of the evaporator 3 through the regulating valve IV 36 and the check valve V26, and when the gas pressure and the temperature in the recovery tank A meet the air inlet requirement of the evaporator 3, the gas is directly sent to the evaporator 3 and does not enter the liquid storage tank 1.
And the recovery tank A and the working medium recovery inlet pipeline are sequentially provided with a check valve I22 and a regulating valve I28 for controlling the parameters of the gas entering the recovery tank A.
The recovery tank A is provided with a pressure measuring point P a, a temperature measuring point T a and a purity measuring point S a for monitoring parameters of recovered working media, a liquid storage tank measuring point P 1 and an evaporator inlet measuring point P 2 for control.
The recovery tank B is consistent with the control method and system configuration of the recovery tank A, and the protection scope is also consistent.
(1) And (3) recycling and controlling the dry gas seal gas entering the compressor 8:
The low-temperature CO 2 working medium from the high-pressure storage tank 7 is firstly sent to the electric heating oil heater H, and the temperature of the outlet gas of the heater is set to be 85-95 ℃. In order to raise the temperature of the low-temperature CO 2 working medium and the existing gas in the discharge pipeline, the gas at the outlet of the heater H is introduced into the compressor chamber through the dry gas seal gas supply pipeline I, the discharge valve 39 of the compressor cylinder body and the discharge valve 38 of the compressor outlet pipeline are opened, all the gas introduced in the compressor 8 is discharged into the discharge pipeline III, and finally the gas enters the recovery tank A through the check valve 22 and the regulating valve 28.
(2) And (3) recycling and controlling dry gas seal gas entering the turbine 9:
And the low-temperature CO 2 working medium from the high-pressure storage tank 7 is sent to the electric heating oil heater H, and the temperature of the gas at the outlet of the heater is set to be 120-135 ℃. The compressor dry gas seal gas and the turbine dry gas seal gas are not put into operation at the same time, so that the temperatures of the outlet gases can be set respectively. In order to raise the temperature of the low-temperature CO 2 working medium and the existing gas in the exhaust pipeline, the gas at the outlet of the heater H is introduced into the turbine chamber through a dry gas seal gas supply pipeline II, a turbine carbon ring protection exhaust valve 40 and a turbine cylinder body exhaust valve 41 are opened at the same time, all the gas introduced in the turbine 9 is discharged into an exhaust pipeline IV, and finally the gas enters a recovery tank B through a check valve II 23 and a regulating valve II 29.
(3) Recovery control of exhaust line three V:
When the filter screen is replaced or equipment is overhauled (including overhauling of each storage tank) after the unit is stopped, all working media in the system are required to be emptied. Firstly, the system is exhausted, the overhaul exhaust of each storage tank is introduced into an exhaust pipeline III V, and is controlled by an inlet regulating valve II 29 of the recovery tank B to enter the recovery tank B before being merged into an inlet check valve II 23 of the recovery tank B through a pneumatic shutoff valve I31 and a check valve II 27. When the recovery tank B is abnormal and cannot be recovered, the pneumatic shutoff valve six 37 is opened, the gas in the exhaust line three V is merged into the exhaust line one III, and finally the gas is recovered to the recovery tank A.
(4) Control of vacuum pump one 16 in recovery tank a:
Before the working medium is recovered, the inlet regulating valve I28 is closed, the tank pneumatic shutoff valve IV 34 is closed, the inlet manual valve 42 of the conveying pump B is closed, the vacuum pump inlet shutoff valve 32 is opened, and the vacuum pump I16 is started. The pressure P a of the recovery tank A is closely monitored after the vacuum pump is started normally, and when P a < -80kPa, the vacuum pump inlet shutoff valve 32 is closed in an interlocking way, and the vacuum pump I16 is stopped.
(5) Control of the compressor motor 20 in recovery tank a:
when recovery tank A draws a vacuum above-80 kPa, vacuum pump one 16 is deactivated and shut-off valve 32 is closed. The manual valve 42 at the inlet of the conveying pump B is kept closed, the pneumatic shutoff valve IV 34 is kept closed, the first 28 pressure of the inlet regulating valve of the recovery tank A is set automatically, the pressure point P a of the tank body is tracked, and the pressure fixed value is set to be 4.5MPa. When P a reaches 4.5MPa, the motor 20 of the compression device is started to compress the working medium recovered in the recovery tank A. After the compressor motor 20 is started, the first cooling device 18 is started in an interlocking manner, and finally the working medium recovered in the recovery tank is compressed, cooled and liquefied. When the pressure of the working fluid in recovery tank a is compressed to P a＞P1 +0.5, compressor motor 20 is shut down.
(6) Control of recovery tank A blowdown valve:
Before the recovery tank is started for the first time, the recovery tank is purged by using the introduced CO 2 working medium, and is purged into the sewage disposal tank A through the pneumatic valve 34, and the discharge valve 34 also has the functions of emergency pressure relief, tank body drainage and gas evacuation. In order to prevent the recovered circulating working medium from carrying impurities such as water vapor, an automatic pollution discharge function of the recovery tank is added, namely, the bottom of the recovery tank is opened every 8 hours to drain the water and the gas for 1 min.
(7) Control of a conveying pump B matched with the recovery tank A:
When the pressure of the working fluid in the recovery tank a P a＞P1 +0.5, the compressor motor 20 is shut down. And opening a manual valve 42 at the inlet of the conveying pump B, opening an inlet regulating valve III 30 of the liquid storage tank 1, keeping the opening of 10-50%, and manually adjusting, and starting the conveying pump at the moment to recover the liquid CO 2 working medium in the recovery tank into the storage tank 1.
When the liquid storage tank 1 fails or the pressure is not matched, and P a＞P2 +0.5, the recovered working medium at the outlet of the delivery pump B can be directly sent to the inlet of the evaporator through the regulating valve IV 36 and the check valve V26.
(8) The control of the recovery tank B and the matched equipment is similar to that of the recovery tank A in the steps (4) - (6).
Claims (4)
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| CN114135353A (en) * | 2021-12-01 | 2022-03-04 | 中国核动力研究设计院 | System and method for starting supercritical carbon dioxide device with fixed quality control |
| CN115978448A (en) * | 2023-01-06 | 2023-04-18 | 茂名华粤华源气体有限公司 | Carbon dioxide emptying waste recycling process |
| CN116293424B (en) * | 2023-03-17 | 2025-07-04 | 西安交通大学 | A dense phase carbon dioxide supply-storage system and method of use thereof |
| CN115993070B (en) * | 2023-03-24 | 2023-07-18 | 百穰新能源科技(深圳)有限公司 | Energy storage system and control method thereof |
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