CN211041017U

CN211041017U - Energy-saving water-saving and cold-heat cogeneration device

Info

Publication number: CN211041017U
Application number: CN201921331257.XU
Authority: CN
Inventors: 王争荣; 王桦; 李伟; 汪洋; 沈明忠
Original assignee: China Huadian Engineering Group Co Ltd; Huadian Environmental Protection Engineering and Technology Co Ltd
Current assignee: China Huadian Engineering Group Co Ltd; Huadian Environmental Protection Engineering and Technology Co Ltd
Priority date: 2019-08-15
Filing date: 2019-08-15
Publication date: 2020-07-17
Anticipated expiration: 2029-08-15

Abstract

The utility model discloses an energy-conserving water conservation and cold and heat cogeneration device, the device through setting up the first circulation circuit of at least one-level and circulation heat exchange pipeline, solve coal fired power plant or other trades dehumidification plume, the problem that deep water lift system only drops into and does not have the income, simultaneously through setting up user side refrigerating system to user side refrigerating system package set up in on the circulation heat exchange pipeline, refrigerating system adopts L iBr heat pump, L iBr heat pump and the parallelly connected setting of heat transfer station in heating season, finally, retrieve the flue gas latent heat through open heat pump system, heating season is used for heating (being heat transfer station) and non-heating season is used for refrigerating (being L iBr heat pump), and the system adopts and sets up closed heat pump at the user, and non-heating season utilizes heating season heat supply circulating pipe to deliver hot water to L iBr heat transfer station, refrigerates as the drive heat source with this hot water, can solve summer heat power plant low-usage, drawback such as the heat network system is idle.

Description

Energy-saving water-saving and cold-heat cogeneration device

Technical Field

The utility model belongs to the technical field of the environmental protection, concretely relates to energy-conserving water conservation and combined cold and heat production device.

Background

At present, the mainstream smoke plume elimination technology is that flue gas condensers and spray towers are arranged behind a desulfurizing tower or slurry coolers are additionally arranged on a slurry circulating slurry pipe to cool flue gas at the outlet of the desulfurizing tower to separate out moisture, and the clean flue gas is heated by using the waste heat of the original flue gas. The cold source is a problem which must be faced by the current mainstream technology in order to take away latent heat of purified flue gas, particularly for areas which stipulate the outlet flue gas temperature and moisture content of a desulfurizing tower, the cold source needs to be condensed in winter or even needs to be condensed in summer, and a water cooling tower in a power plant is always operated at full load in summer, so that an effective cold source cannot be provided, if investment is required to be increased for newly-built water cooling towers, waste water is replaced by good water, and a water-saving effect cannot be achieved. If the new mechanical ventilation cooling tower is built, the construction cost is extremely high, and the new mechanical ventilation cooling tower cannot bear a power plant. The existing mainstream technology has the defects of energy and water resource waste and high investment cost, so that only investment is needed for eliminating the wet smoke plume without benefit.

In winter, the output hot water of the thermal power plant is conveyed to a heat exchange station of a user through a city centralized heat supply pipeline, and the exchanged hot water is sent to the home of the user through a secondary pipe network. In summer, the heat load demand of heat consumers is very small, and most heating systems are idle or provide load for individual consumers with domestic hot water demand. The heat supply quantity of the part can not reach the heat supply capacity of the thermal power plant, so that the utilization rate of the heat supply pipe network is very low in the current situation in non-heating seasons. The heat supply load in summer is lower, which causes the increase of the heat dissipation loss of the pipe network and the increase of the operation cost, and leads to the increase of the cost of unit heat. The heating units of many thermal power plants can only be shut down or operated in a pure steam mode during the non-heating season due to the low thermal load during the non-heating season. The combined heat and power generation is used as an efficient energy production mode, and the energy utilization rate can reach more than 70%. However, in the pure condensing operation mode, the energy utilization rate is only about 35%, so that the advantage of the energy utilization rate of the cogeneration is buried.

At present, most buildings adopt electric air-conditioning refrigeration, and a plurality of centralized electric air-conditioners used by large-scale public buildings comprise public buildings such as hospitals, hotels, department stores, hotels and the like. The large-scale use of electric air conditioning refrigeration is one of the reasons for peak load of electric power in summer. To cope with the peak power load, the power transmission and distribution system has to be expanded. The capacity of the newly added transformer is only used as power peak regulation in summer, and power loads cannot reach the maximum installed capacity at other times, and meanwhile, partial transformer idleness is caused, and resource waste is caused.

Utilize current thermal power plant and hot-water pipe network to supply cold for the user in summer, both can reduce summer air conditioning equipment to electric power system's dependence, effectively reduce city summer electric power demand peak value, can increase summer load again, improve the utilization ratio of current heating equipment and heat supply pipe network, increase heating system's economic benefits.

At present, the common centralized cooling method is to produce chilled water in a thermal power plant and send the chilled water to each air-conditioning user for use through a centralized heat supply pipeline. Because the large-scale thermal power plant is far away from the city center, the temperature difference between the supply water and the return water of the air conditioner is very small (generally about 5 ℃), thereby causing the increase of the operation cost and the heat loss of the system.

SUMMERY OF THE UTILITY MODEL

Therefore, the to-be-solved technical problem of the utility model is that the energy-conserving water conservation of large-scale steam power plant and cold and heat cogeneration eliminate in coordination that wet smoke plume exists that the system operating cost and heat loss rise and the idle scheduling problem of the low heat supply network of non-heating season load. The flue gas after wet desulphurization is saturated flue gas at about 50 ℃, a large amount of saturated water and free water are carried in the flue gas, and if the flue gas is directly discharged from a chimney, the visual pollution of wet smoke plume can be caused, and a large amount of water resources and latent heat of water vapor in the flue gas are wasted.

Therefore, the utility model provides an energy-saving water-saving and cold-heat cogeneration device, which comprises a dust removal device, a desulphurization device and an absorption device which are sequentially communicated and arranged, and also comprises,

the liquid inlet end of the first circulation loop is communicated with the lower part of the absorption device, and the liquid outlet end of the first circulation loop is communicated with the upper part of the absorption device, so that the liquid at the liquid outlet end enters the absorption device and is in countercurrent contact with the flue gas entering the absorption device;

the circulating heat exchange pipeline is intersected with the first circulating loop through a second heat exchanger;

the user side refrigeration system comprises L iBr heat pumps which are all arranged on a circulating heat exchange pipeline, wherein the L iBr heat pump is connected with an original heating heat exchange station in parallel, heating seasonal heat network circulating water is used for heating secondary heat network water of the heat exchange station, so that secondary pipe network hot return water from a user is subjected to heat exchange through the heat exchange station to form secondary pipe network hot outlet water and returns the secondary pipe network hot outlet water to the user for heating of the user, the heat network water after heat exchange returns to an open type absorption heat pump system, the heat network water is switched to a L iBr heat pump when no heat supply requirement exists in non-heating seasons, the heat network water serves as a driving heat source, the heat network water after heat exchange returns to the open type absorption heat pump system, the L iBr heat pump is used for refrigerating the user, and refrigerant return water from the user is subjected to heat exchange through the L iBr heat.

The flue gas treatment device further comprises a liquid storage unit which is arranged in the absorption device and divides the inner cavity of the absorption device into a first flue gas treatment area and a second flue gas treatment area, and the flue gas is suitable for entering the second flue gas treatment area from the first flue gas treatment area through the liquid storage unit;

and the liquid inlet end of the first heat exchanger is communicated with the liquid storage unit, and the liquid outlet end of the first heat exchanger is communicated with the first flue gas treatment area close to the liquid storage unit, so that the solution in the liquid storage unit enters the first heat exchanger for heat exchange, and the solution after heat exchange is sent into the first flue gas treatment area to be contacted with the flue gas.

The liquid outlet end of the second circulation loop is communicated with the upper part of the absorption device, so that the liquid which is regenerated by the regeneration system and enters the absorption device from the liquid outlet end enters the absorption device and is in countercurrent contact with the flue gas entering the absorption device.

Further, the regeneration system comprises a flash tank, wherein a dilute solution inlet is arranged at the upper part of the flash tank, a steam outlet is arranged at the upper part of the flash tank, and a concentrated solution outlet is arranged at the lower part of the flash tank;

the lower part of the absorption device, the sixth heat exchanger, the seventh heat exchanger and the dilute solution inlet are sequentially communicated, and the concentrated solution outlet, the sixth heat exchanger, the fifth heat exchanger and the upper part of the absorption device are communicated, so that the concentrated solution and the solution from the lower part of the absorption device enter the upper part of the absorption device after heat exchange in the sixth heat exchanger.

The concentrated solution outlet, the sixth heat exchanger, the fifth heat exchanger and the first spraying unit are sequentially communicated and arranged so as to spray the concentrated solution after heat exchange on the rising flue gas through the first spraying unit;

and the second spraying unit is arranged in the absorption device close to and below the liquid storage unit, and the liquid storage unit, the first heat exchanger and the second spraying unit are sequentially communicated so as to spray the solution contacted with the flue gas onto the clean flue gas after heat exchange and realize counter-current convection with the clean flue gas.

The lower part of the absorption device, the solution filtering and conditioning system, the second heat exchanger, the first spraying unit and/or the second spraying unit are sequentially communicated and arranged, so that dilute solution is sent into the first spraying unit and/or the second spraying unit after being subjected to filtering, conditioning and heat exchange.

The first heat exchanger, the second heat exchanger, the third heat exchanger, the fourth heat exchanger and the user side refrigerating system are communicated in sequence, so that incoming water or low-condensation water of a heat supply network sequentially passes through the first heat exchanger, the second heat exchanger, the third heat exchanger and the fourth heat exchanger and exchanges heat with substances entering the corresponding heat exchangers, and hot water of a pipe network from the fourth heat exchanger is used as a heat exchange medium of the user side refrigerating system.

Further, the seventh heat exchanger is communicated with the third heat exchanger, so that condensate water extracted by the steam turbine after heat exchange of the seventh heat exchanger is used as a heat exchange medium of the third heat exchanger, and a steam return machine performs low pressure heating after heat exchange;

the steam outlet is communicated with the fourth heat exchanger so that secondary steam from the steam outlet is used as a heat exchange medium of the fourth heat exchanger, and condensed water after heat exchange is used for process water replenishing.

The outlet of the fourth heat exchanger is communicated with the economizer so as to exchange heat between pipe network hot water and the flue gas from the dust removal device in the economizer, the flue gas after heat exchange is sent into the desulfurization device, and the pipe network hot water after heat exchange is sent into the user side refrigeration system.

Furthermore, the lower part of the absorption device is provided with a flue gas inlet, the upper part of the absorption device is provided with a flue gas outlet, the flue gas outlet is communicated with the chimney, and the first spraying unit, the liquid storage unit and the second spraying unit are all positioned between the flue gas inlet and the flue gas outlet;

the demister is arranged in the absorption device and is positioned between the first spraying unit and the flue gas outlet.

The utility model discloses technical scheme has the following advantage, through setting up at least one-level first circulation circuit and circulation heat exchange pipeline, solves coal fired power plant or other trades and disappears the problem that dehumidification plume, degree of depth water lift system only drop into and do not have the income, simultaneously through setting up user side refrigerating system, and this user side refrigerating system package set up in on the circulation heat exchange pipeline, refrigerating system adopts L iBr heat pump, L iBr heat pump sets up with the heat transfer station of heating season parallelly connected, finally, retrieve the latent heat of flue gas through open heat pump system, the heating season is used for heating (being the heat transfer station) and non-heating season is used for refrigerating (being L iBr heat pump), the system adopts and sets up closed heat pump at the user, non-heating season utilizes heating season heat supply circulating pipe to deliver hot water to L iBr station, uses this hot water as the drive heat source to refrigerate, can solve summer heat power plant low-usage, drawback such as the heat network system is idle to can partially alleviate city in summer and use the shortage of electricity and once problem such as energy consumption, reach environmental protection effect such as efficient emission reduction energy conservation.

Drawings

In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the embodiments or the technical solutions in the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.

Fig. 1 is a system diagram of an energy-saving and water-saving combined cooling and heating device in an embodiment of the present invention;

FIG. 2 is a schematic view of the absorbent device of FIG. 1;

FIG. 3 is another system diagram of the energy-saving water-saving and combined cooling and heating apparatus according to the embodiment of the present invention;

FIG. 4 is a schematic view of the absorbent device of FIG. 3;

wherein the reference numerals are represented as:

the method comprises the following steps of 1-dedusting device, 2-desulphurization device, 3-absorption device, 3-1-first spraying unit, 3-2-second spraying unit, 3-3-liquid storage unit, 3-4-flue gas inlet, 3-5-flue gas outlet, 3-6-demister, 4-economizer, 5-chimney, 6-solution filtration conditioning system, 7-first heat exchanger, 8-second heat exchanger, 9-third heat exchanger, 10-fourth heat exchanger, 11-fifth heat exchanger, 12-sixth heat exchanger, 13-seventh heat exchanger, 14-flash tank, 15-user side refrigerating system, 15-0-heat net initial station, 15-1-heat exchange station, 15-2-L iBr heat pump and 16-user.

Detailed Description

The technical solutions of the present invention will be described clearly and completely below, and it should be apparent that the described embodiments are some, but not all embodiments of the present invention. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.

In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplification of description, but do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.

In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art.

Furthermore, the technical features mentioned in the different embodiments of the invention described below can be combined with each other as long as they do not conflict with each other.

Example 1

The embodiment provides an energy-saving water-saving and combined cooling and heating device, as shown in fig. 1 and 2, comprising a dust removing device 1, a desulfurizing device 2 and an absorbing device 3 which are sequentially communicated, wherein, if the dust removing device 1 can be an electric dust remover, the desulfurizing device 2 can be a desulfurizing tower, the absorbing device 3 can be an absorbing tower, the lower part of the absorbing device 3 is provided with a flue gas inlet 3-4, the upper part is provided with a flue gas outlet 3-5, and the device further comprises,

the liquid inlet end of the first circulation loop is communicated with the lower part of the absorption device 3, and the liquid outlet end of the first circulation loop is communicated with the upper part of the absorption device 3, so that liquid at the liquid outlet end enters the absorption device 3 and is in countercurrent contact with the flue gas entering the absorption device 3; in this embodiment, the number of the first circulation loops is two;

a circulating heat exchange pipeline which is intersected with the first circulating loop through a second heat exchanger 8; in this embodiment, two second heat exchangers 8 are provided, and are arranged in series in the first circulation loop, and the number of the second heat exchangers 8 corresponds to the number of the first circulation loop;

the user side refrigerating system 15 comprises a heat exchange station 15-1 and a L iBr heat pump 15-2 which are arranged on a circulating heat exchange pipeline, the heat exchange station 15-1 and a L iBr heat pump 15-2 are arranged in parallel, so that secondary pipe network hot return water from a user forms secondary pipe network hot outlet water and is recycled to the user after heat exchange is carried out through the heat exchange station 15-1, refrigerant return water from the user forms refrigerant outlet water and is recycled to the user after heat exchange is carried out through a L iBr heat pump 15-2, a heat exchange medium from a second heat exchanger 8 forms refrigerant outlet water and returns to the second heat exchanger 8 after passing through the heat exchange station 15-1 and the L iBr heat pump 15-2, specifically, the user side refrigerating system comprises L iBr heat pumps which are arranged on the circulating heat exchange pipeline, a L iBr heat pump is arranged in parallel with an original heating heat exchange station, the heating season heat network circulating water is used for heating heat exchange station secondary heat network water, so that the secondary pipe network hot return water from the user forms secondary pipe network hot outlet water and returns to the user after heat exchange is carried out through the heating heat exchange station, the open heat pump system is used for heat exchange, the user heat pump heat exchange water is used for absorbing heat pump heat exchange, and is used for absorbing heat pump heat exchange, the heat pump system is used for absorbing heat pump heat source heat pump.

In the energy-saving water-saving and cold-heat cogeneration device, the problems that a coal-fired power plant or other industries eliminate wet smoke plume and a deep water lifting system is only put into use and does not have benefit are solved by arranging at least one stage of first circulation loop and a circulation heat exchange pipeline, meanwhile, a user side refrigerating system 15 is arranged, the user side refrigerating system 15 comprises a heat exchange station 15-1 and a L iBr heat pump 15-2 which are arranged on the circulation heat exchange pipeline, the heat exchange station 15-1 and the L iBr heat pump 15-2 are arranged in parallel, secondary pipe network hot return water from a user is subjected to heat exchange through the heat exchange station 15-1 by the user side refrigerating system 15 to form secondary pipe network hot outlet water and is recycled to the user, refrigerant return water from the user is subjected to heat exchange through a L iBr heat pump 15-2 to form refrigerant outlet water and is recycled to the user, a heat exchange medium from the second heat exchanger 8 returns to the second heat exchanger 8 after passing through the heat exchange stations 15-1 and L iBr heat pump 15-2, finally, latent heat in a heat pump system (namely, a closed heat exchange station or an open heat pump is used for closed type heat exchange system or an open type heat pump, the heat pump is used for achieving the purposes of energy saving, the environment-saving and reducing effect of a low-saving system, the environment-saving effect and the environment-saving effect of the.

Example 2

The embodiment provides an energy-saving water-saving and combined cooling and heating device, based on embodiment 1, as shown in fig. 3 and 4, the device further comprises a liquid storage unit 3-3, for example, the liquid storage unit 3-3 can be a liquid receiving disc, as shown in fig. 4, the liquid receiving disc is provided with a disc adapted to an inner cavity of a desulfurization tower, a through hole is formed in the disc, the through hole is provided with an extending section extending towards the top of the desulfurization tower along the axial direction of the desulfurization tower, a liquid storage space is formed between adjacent extending sections, the absorbing device 3 is arranged and divides the inner cavity into a first flue gas treatment area and a second flue gas treatment area, and flue gas is suitable for entering the second flue gas treatment area from the first flue gas treatment area through the liquid storage unit 3-3; specifically, the liquid storage unit 3-3 may be disposed in the middle of the desulfurization tower;

and the liquid inlet end of the first heat exchanger 7 is communicated with the liquid storage unit 3-3, and the liquid outlet end of the first heat exchanger is communicated with the first flue gas treatment area close to the liquid storage unit 3-3, so that the solution in the liquid storage unit 3-3 enters the first heat exchanger 7 for heat exchange, and the solution after heat exchange is sent to the first flue gas treatment area to be contacted with the flue gas.

The device further comprises a second circulation loop, wherein a regeneration system is arranged on the second circulation loop, the liquid inlet end of the second circulation loop is communicated with the lower part of the absorption device 3, and the liquid outlet end of the second circulation loop is communicated with the upper part of the absorption device 3, so that liquid regenerated by the regeneration system and discharged from the liquid outlet end enters the absorption device 3 and is in countercurrent contact with the flue gas entering the absorption device 3;

preferably, the regeneration system includes a flash tank 14, the upper portion of which is provided with a dilute solution inlet and a steam outlet, and the lower portion of which is provided with a concentrated solution outlet; the sixth heat exchanger 12 and the seventh heat exchanger 13, the lower part of the absorption device 3, the sixth heat exchanger 12, the seventh heat exchanger 13 and the dilute solution inlet are sequentially communicated, and the concentrated solution outlet, the sixth heat exchanger 12, the fifth heat exchanger 11 and the upper part of the absorption device 3 are communicated, so that the concentrated solution and the solution from the lower part of the absorption device 3 enter the upper part of the absorption device 3 after heat exchange occurs in the sixth heat exchanger 12.

Due to different water temperature demands of heat supply networks in various regions, if the water temperature of the heat supply network from the open type absorption heat pump system does not meet the heating requirement, the water of the heat supply network continuously enters the heat supply network initial station 15-0 to continuously heat up, the water temperature reaches the heating temperature in the heating season, the higher the water temperature is in the non-heating season, the higher the refrigerating efficiency of the user side closed type heat pump is, the heating in the heating season and the cooling in the non-heating season of the cogeneration unit are realized, and the unit can be kept in a high-load operation state all the year round. After the open type absorption heat pump heats the heat supply network water, the heat supply network water can be directly sent to a heat supply network initial station 15-0, and also can be sent to a coal economizer (such as a low-temperature coal economizer) to further exchange heat with the raw flue gas at the inlet of the desulfurizing tower, so that the problem of hot water can be further improved, and meanwhile, the heat of the raw flue gas is recovered. The existing thermal power plant and hot water pipe network are used for conveying hot water, the hot water is used as a driving heat source of an absorption refrigerating unit in an energy center or a heating station at a user side to prepare chilled water, and then the chilled water is uniformly sent to each air conditioner user through a secondary pipe network for use. Therefore, the problem of heat loss in long-distance transmission is solved, an electric air conditioner can be replaced, the effect of adjusting the power peak value in summer is achieved, the utilization rate of the existing heating equipment and the existing heating pipe network is improved, and the economic benefit of a heating system is increased.

In the energy-saving water-saving and cold-heat co-production device, a liquid storage unit 3-3 is arranged in an absorption device 3, an inner cavity is divided into a first smoke treatment area and a second smoke treatment area by using the liquid storage unit, smoke enters from the bottom of the absorption device 3 and is in countercurrent contact with concentrated solution (such as concentrated salt solution) sprayed on the top of the absorption device 3, the concentrated solution in the second smoke treatment area absorbs the moisture in the smoke and becomes thinner, latent heat released in the phase change process of the moisture is separated out, and the smoke and the concentrated solution are heated to 55-65 ℃; the heated concentrated solution is led out through the liquid storage unit 3-3 to enter a first heat exchanger 7 to exchange heat with a heat exchange medium (such as heat supply network water), the heat exchange medium can be heated by 3-10 ℃, the concentrated solution enters a first flue gas treatment area after being cooled to be approximately consistent with the temperature of a solution inlet at the top of a second flue gas treatment area to continuously absorb moisture in the flue gas, the dilute solution at the bottom of the lower section of the absorption device 3 is respectively sent to a second heat exchanger 8 and a sixth heat exchanger 12 by a dilute salt solution pump, the heat supply network water which is discharged from the first heat exchanger 7 exchanges heat with the dilute solution which enters the second heat exchanger 8, the dilute solution at the bottom of the lower section is cooled to be consistent with the temperature of a solution outlet of the first heat exchanger 7 and mixed with the solution at the outlet of the first heat exchanger 7 to enter the top of the lower section of the absorption device 3 to be sprayed to 50-60 ℃, the, the primary heat exchanger and the secondary heat exchanger of the absorption device 3 are used for cascade heat exchange, so that the quality of heat exchange can be effectively improved; the dilute solution entering the sixth heat exchanger 12 exchanges heat with the concentrated solution from the regeneration system and then enters the regeneration system, the dilute solution heated by the concentrated solution enters a seventh heat exchanger 13 (for example, a plate heat exchanger) to be continuously heated to 120-140 ℃ (the driving heat source is steam of the pump unit), and then flash evaporation is carried out by a flash tank 14. The extracted condensed water enters a third heat exchanger 9 to exchange heat with heat supply network water, the secondary steam at the top of a flash tank 14 enters a fourth heat exchanger 10 to raise the temperature of the heat supply network water to about 85 ℃ for heating or centralized refrigeration, or the secondary steam is connected with a low-low temperature economizer in series to continuously raise the temperature to 90-100 ℃, and the cooled secondary steam condensed water can be used for washing water of a demister of a desulfurizing tower and the like. The concentrated solution at the bottom of the flash tank 14 exchanges heat with the dilute solution in the sixth heat exchanger 12, is cooled to 30-50 ℃ by the fifth heat exchanger 11, and returns to the top of the upper section of the absorption device for recycling.

In this embodiment, the device further comprises a first spraying unit 3-1, which is arranged in the absorption device 3 near the middle upper part and above the liquid storage unit 3-3, and the concentrated solution outlet, the sixth heat exchanger 12, the fifth heat exchanger 11 and the first spraying unit 3-1 are sequentially communicated with each other, so that the concentrated solution after heat exchange is sprayed on the rising flue gas through the first spraying unit 3-1; the second spraying unit 3-2 is arranged in the absorption device 3 and is close to and below the liquid storage unit 3-3, and the liquid storage unit 3-3, the first heat exchanger 7 and the second spraying unit 3-2 are communicated in sequence so as to spray the solution contacted with the flue gas on the clean flue gas after heat exchange so as to perform counter-current flow with the clean flue gas; specifically, the first spraying unit 3-1 and the second spraying unit 3-2 both comprise spraying conduits and spraying nozzles arranged on the spraying conduits at intervals, and the first spraying unit 3-1 and the second spraying unit 3-2 are respectively close to the flue gas outlet 3-5 of the absorption device 3 or a liquid receiving disc and are positioned below the flue gas outlet 3-5 or the liquid receiving disc, so that the countercurrent contact path is prolonged, and the heat in the flue gas can be effectively recovered. An absorber is arranged behind the desulfurizing tower, and the respective spraying layers of the upper section and the lower section can be provided with standby layers so as to improve the reliability of the absorber.

Further, the system also comprises a third heat exchanger 9 and a fourth heat exchanger 10, wherein the first heat exchanger 7, the second heat exchanger 8, the third heat exchanger 9, the fourth heat exchanger 10 and the user side refrigerating system 15 are sequentially communicated, so that incoming water or low-condensation water of a heat supply network sequentially passes through the first heat exchanger 7, the second heat exchanger 8, the third heat exchanger 9 and the fourth heat exchanger 10 and exchanges heat with substances entering the corresponding heat exchangers, and hot water of the pipe network coming out of the fourth heat exchanger 10 is used as a heat exchange medium of the user side refrigerating system 15.

Further, the seventh heat exchanger 13 is communicated with the third heat exchanger 9, so that the steam extracted by the steam turbine after heat exchange in the seventh heat exchanger 13 is condensed as a heat exchange medium of the third heat exchanger 9, and the steam return turbine is low-pressure fed after heat exchange;

the steam outlet is communicated with the fourth heat exchanger 10, so that secondary steam from the steam outlet is used as a heat exchange medium of the fourth heat exchanger 10, and condensed water after heat exchange is used for process water replenishing.

In addition, a fifth heat exchanger 11 is also arranged, and the concentrated solution from the sixth heat exchanger 12 can enter the fifth heat exchanger 11 to exchange heat with heat supply network water or low-pressure condensate water and then enter the absorption device 3.

Example 3

The embodiment provides an energy-saving water-saving and combined cooling and heating device, on the basis of the embodiment 1 or 2, in order to filter and modulate the concentrated absorption liquid in the absorption device, the device further comprises a solution filtering conditioning system 6, wherein the lower part of the absorption device 3, the solution filtering conditioning system 6, a second heat exchanger 8, a first spraying unit 3-1 and/or a second spraying unit 3-2 are sequentially communicated and arranged, so that the dilute solution is sent to the first spraying unit 3-1 and/or the second spraying unit 3-2 after being subjected to filtering conditioning and heat exchange; specifically, the solution filtering and conditioning system 7 consists of a cyclone and a filter which are sequentially communicated, and a solution supplementing tank and a fifth pump which are sequentially communicated are arranged at the same time, and the fifth pump is communicated with the solution filtering and conditioning system so as to supplement the solution into the solution filtering and conditioning system.

Example 4

In the embodiment, on the basis of the embodiments 1 to 3, in order to realize the flow of liquid, a first pump is arranged between the lower part of the absorption device 3 and the second heat exchanger 8 or between the second heat exchanger 8 and the second spraying unit 3-2; a second pump is arranged between the lower part of the absorption device 3 and the solution filtering and tempering system 6, or between the solution filtering and tempering system 6 and the second heat exchanger 8, or between the second heat exchanger 8 and the second spraying unit 3-2; a third pump is arranged between the lower part of the absorption device 3 and the sixth heat exchanger 12, or between the sixth heat exchanger 12 and the seventh heat exchanger 13, or between the seventh heat exchanger 13 and the flash tank 14; and a fourth pump is arranged between the concentrated solution outlet and the sixth heat exchanger 12 or between the sixth heat exchanger 12 and the first spraying unit 3-1.

And in non-heating seasons when no heating demand exists, the heat supply network water is switched to L iBr heat pumps, the heat supply network water is used as a driving heat source, the heat exchange heat supply network water returns to an open type absorption heat pump system, a L iBr heat pump is used for refrigerating a user, and refrigerant return water from the user forms refrigerant outlet water after heat exchange through the L iBr heat pump and is recycled to the user.

Example 5

This embodiment provides an energy-conserving water conservation and cold and heat cogeneration device, on the basis of above-mentioned embodiment 1, 2, 3 or 4, still include economizer 4, set up between dust collector 1 and desulphurization unit 2, the export of fourth heat exchanger 10 communicates with economizer 4 to exchange heat in economizer 4 with the flue gas that comes from dust collector 1 with pipe network hot water, and send into desulphurization unit 2 with the flue gas after the heat transfer, pipe network hot water after the heat transfer sends into user side refrigerating system 15.

Furthermore, the lower part of the absorption device 3 is provided with a flue gas inlet 3-4, the upper part is provided with a flue gas outlet 3-5, the flue gas outlet 3-5 is communicated with a chimney 5, and the first spraying unit 3-1, the liquid storage unit 3-3 and the second spraying unit 3-2 are all positioned between the flue gas inlet 3-4 and the flue gas outlet 3-5; the demister 3-6 is arranged in the absorption device 3 and is positioned between the first spraying unit 3-1 and the flue gas outlet 3-5.

If the smoke temperature needs to be raised to a higher temperature, a reheating heat exchanger can be arranged on a flue behind a smoke outlet 3-5 of the absorption device 3 or a heat exchange pipe is arranged in the top of the upper section of the absorption device 3, so that the smoke temperature can be heated to the temperature required by environmental protection or owners.

In addition, the specific working principle of the above device is as follows:

an absorption tower is arranged behind the desulfurizing tower, flue gas enters from the bottom of the absorption tower and flows against strong salt solution sprayed from the top of the absorption tower, the strong salt solution at the top of the upper section of the absorption tower absorbs the flue gas to dilute, latent heat is released in the phase change process of precipitated moisture, the flue gas and the salt solution are heated, and the flue gas and the salt solution are heated to 55-65 ℃. The heated solution is led out through a liquid receiving disc at the bottom of the upper section to enter a first-stage heat exchanger of a heat supply network (namely a first heat exchanger) to exchange heat with heat supply network water, the heat supply network water can be heated by about 3-10 ℃, a saline solution is cooled to be consistent with the temperature of a solution inlet at the top of the upper section and then enters the top of the lower section of an absorption tower to continuously absorb moisture in flue gas, a dilute solution at the bottom of the lower section of the absorption tower is respectively sent to a second-stage heat exchanger of the heat supply network (namely a second heat exchanger) and a dilute solution heat exchanger of a dilute concentrated solution (namely a fifth heat exchanger) by a dilute saline solution pump, the heat supply network water which is discharged from the first-stage heat exchanger of the heat supply network exchanges heat with the dilute solution which enters the second-stage heat exchanger (namely the second heat exchanger), the dilute solution at the bottom of the lower section is cooled to be consistent with the temperature of a solution, the technology considers the temperature gradient from the top to the bottom of the absorber, and the first-stage heat exchanger and the second-stage heat exchanger of the absorber perform cascade heat exchange, so that the quality of heat exchange can be effectively improved; the dilute solution entering the dilute-concentrated solution heat exchanger exchanges heat with the concentrated solution from the regeneration system and then enters the regenerator system. And (3) enabling the dilute solution heated by the concentrated solution to enter a plate heat exchanger to be continuously heated to 120-140 ℃, driving a heat source to adopt steam of a pump unit, then carrying out flash evaporation of a flash tank, enabling condensed water obtained after the extracted steam is subjected to heat exchange through the plate heat exchanger to enter a heat supply network three-level heat exchanger (a third heat exchanger) to exchange heat with heat supply network water at a heat supply network second-level outlet, heating the heat supply network water to 65-75 ℃, and returning the cooled condensed water to a low-pressure heating system. The secondary steam at the top of the flash tank enters a heat supply network four-stage heater (namely a fourth heat exchanger) to exchange heat with heat supply network water at the outlet of the heat supply network three-stage heat exchanger, the temperature is raised to 85-95 ℃, and the obtained hot water is used for heating in the heating season and is used for refrigerating in the non-heating season; the concentrated solution at the bottom of the flash tank exchanges heat with the dilute solution in a dilute concentrated solution heat exchanger, and then is cooled to 30-50 ℃ through a concentrated solution cooling heat exchanger and returns to the top of the upper section of the absorption tower for recycling.

The bottom of the lower section of the absorption tower is matched with a filtering and tempering unit, on one hand, solid particles accumulated in the absorber by the solution and generated substances such as crystal salt (sulfate, carbonate and the like) can be removed through the cyclone and the filtering device, so that pollutants and impurities in the solution of the absorber are controlled to a certain degree; on the other hand, alkali salt is added to adjust the pH value of the solution, maintain the absorption capacity of the solution and reduce the corrosivity of the solution; and the lost solution can be replenished through a conditioning system. Meanwhile, an absorption tower is arranged behind the desulfurizing tower, flue gas enters from the bottom of the absorption tower and flows against a strong salt solution sprayed from the top of the absorption tower, the strong salt solution at the top of the upper section of the absorption tower absorbs moisture in the flue gas and becomes thinner, latent heat is released in the phase change process of the separated moisture, the flue gas and a salt solution are heated to 55-65 ℃, if the flue gas temperature needs to be raised to a higher temperature, a reheating heat exchanger can be arranged on a flue behind the absorption tower or a heat exchange tube is arranged in the top of the upper section of the absorption tower, and the flue gas temperature is heated to the temperature required by environmental protection or an owner.

An absorption tower is arranged behind the desulfurizing tower, the water content of clean flue gas can be greatly reduced through the absorption tower, and the dryness and temperature of the flue gas can be improved due to latent heat released by phase change in the absorption process of steam, so that wet smoke plume elimination, deep water lifting, dust content reduction of the flue gas and low-quality latent heat of the steam in the recovered flue gas can be simultaneously achieved. One part of the absorbed dilute solution is cooled to the temperature of the concentrated solution through a dilute concentrated solution heat exchanger (namely, a fifth heat exchanger), the other part of the absorbed dilute solution can be used for heating heat supply network water through a heat supply network water secondary heat exchanger, and the flow sizes of the two streams are adjusted according to specific requirements. The dilute solution is recovered to the original concentration through a regeneration system, the concentrated solution is conveyed to an absorber behind the desulfurizing tower again, the regeneration system adopts a unit to pump air, condensed water returns to the boiler for water supply, and secondary steam condensed water is used for process water supplement of the desulfurizing tower. After the heat supply network water or the low condensed water is subjected to heat exchange and temperature rise through the first-stage heat exchanger and the second-stage heat exchanger of the absorber, the heat supply network water or the low condensed water is subjected to heat exchange with the third-stage heat exchanger and the fourth-stage heat exchanger of the regeneration system, and the requirement of the temperature of the heat supply network water in the heating season or the requirement of the heat pump for centralized refrigeration. Because the flue gas water content at the bottom of the absorption tower is high, most water absorption occurs at the part, the bottom of the absorption tower is provided with a small circulation, the lower section balance temperature of the absorption tower is controlled by reducing the temperature of a small circulation solution, so that the water absorption capacity of a unit mass solution is improved, the concentration of the absorbed dilute solution is reduced by 1-10% relative to that of a concentrated solution, and the volume ratio of the small circulation volume to the regeneration circulation volume can be 1:1-10: 1.

It should be understood that the above examples are only for clarity of illustration and are not intended to limit the embodiments. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. And are neither required nor exhaustive of all embodiments. And obvious variations or modifications can be made without departing from the scope of the invention.

Claims

1. An energy-saving water-saving cold and heat cogeneration device, which comprises a dust removal device, a desulphurization device and an absorption device which are sequentially communicated, and is characterized by also comprising a desulfurization device,

the user side refrigeration system comprises L iBr heat pumps which are all arranged on a circulating heat exchange pipeline, wherein a L iBr heat pump is arranged in parallel with an original heating heat exchange station, heating seasonal heat supply network circulating water is used for heating secondary heat supply network water of the heat exchange station, so that secondary pipe network hot return water from a user forms secondary pipe network hot outlet water after heat exchange through the heat exchange station and returns to the user for heating of the user, the heat supply network water after heat exchange returns to an open type absorption heat pump system, the heat supply network water is switched to a L iBr heat pump when no heat supply demand exists in a non-heating season, the heat supply network water is used as a driving heat source, the heat supply network water after heat exchange returns to the open type absorption heat pump system, the L iBr heat pump is used for refrigerating the user, and refrigerant return water from the user forms refrigerant outlet water after heat exchange through the L iBr heat pump.

2. The combined cooling, heating and power generation apparatus according to claim 1, further comprising a liquid storage unit disposed in said absorption apparatus and dividing an inner cavity thereof into a first flue gas treatment zone and a second flue gas treatment zone, wherein flue gas is adapted to pass from said first flue gas treatment zone through said liquid storage unit into said second flue gas treatment zone;

3. The apparatus according to claim 2, further comprising a second circulation loop, wherein a regeneration system is disposed on the second circulation loop, and a liquid inlet end of the second circulation loop is communicated with a lower portion of the absorption apparatus, and a liquid outlet end of the second circulation loop is communicated with an upper portion of the absorption apparatus, so that the liquid regenerated by the regeneration system and flowing from the liquid outlet end enters the absorption apparatus and is in countercurrent contact with the flue gas entering the absorption apparatus.

4. The energy-saving water-saving and combined heat and cold production apparatus according to claim 3, wherein the regeneration system comprises,

a dilute solution inlet is arranged in the middle of the flash tank, a steam outlet is arranged at the upper part of the flash tank, and a concentrated solution outlet is arranged at the lower part of the flash tank;

5. The energy-saving water-saving cold and heat cogeneration apparatus according to claim 4, further comprising,

the first spraying unit is arranged in the absorption device close to the middle upper part of the absorption device and is positioned above the liquid storage unit, and the concentrated solution outlet, the sixth heat exchanger, the fifth heat exchanger and the first spraying unit are sequentially communicated so as to spray the concentrated solution after heat exchange on the rising flue gas through the first spraying unit;

6. The energy-saving water-saving cold and heat cogeneration device according to claim 5, further comprising a solution filtering conditioning system, wherein the lower part of the absorption device, the solution filtering conditioning system, the second heat exchanger, the first spraying unit and/or the second spraying unit are sequentially communicated and arranged so as to send the dilute solution into the first spraying unit and/or the second spraying unit after the filtering conditioning and the heat exchange.

7. The energy-saving water-saving and cold-heat cogeneration apparatus according to claim 5 or 6, further comprising,

the first heat exchanger, the second heat exchanger, the third heat exchanger, the fourth heat exchanger and the user side refrigerating system are communicated in sequence, so that water coming from a heat supply network or low-condensation water sequentially passes through the first heat exchanger, the second heat exchanger, the third heat exchanger and the fourth heat exchanger and exchanges heat with substances entering the corresponding heat exchangers, and pipe network hot water coming out of the fourth heat exchanger is used as a heat exchange medium of the user side refrigerating system.

8. The energy-saving water-saving cold and heat cogeneration device according to claim 7, wherein the seventh heat exchanger is communicated with the third heat exchanger so that the condensate water extracted by the steam turbine after heat exchange of the seventh heat exchanger is used as a heat exchange medium of the third heat exchanger, and the steam turbine is fed back after heat exchange;

9. The energy-saving water-saving cold and heat cogeneration apparatus according to claim 8, further comprising,

the economizer is arranged between the dust removal device and the desulfurization device, an outlet of the fourth heat exchanger is communicated with the economizer so as to exchange heat between pipe network hot water and flue gas from the dust removal device in the economizer, the flue gas after heat exchange is sent into the desulfurization device, and the pipe network hot water after heat exchange is sent into the user side refrigeration system.

10. The apparatus for energy saving, water saving, combined cooling and heating as claimed in claim 9, wherein the absorption apparatus has a flue gas inlet at a lower portion thereof and a flue gas outlet at an upper portion thereof, the flue gas outlet is communicated with a chimney, and the first spraying unit, the liquid storage unit and the second spraying unit are all located between the flue gas inlet and the flue gas outlet;