CN107726672B - Premixing continuous variable temperature distillation generator and absorption type circulating system - Google Patents

Premixing continuous variable temperature distillation generator and absorption type circulating system Download PDF

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CN107726672B
CN107726672B CN201710953229.0A CN201710953229A CN107726672B CN 107726672 B CN107726672 B CN 107726672B CN 201710953229 A CN201710953229 A CN 201710953229A CN 107726672 B CN107726672 B CN 107726672B
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heat exchange
tube
exchange tube
outlet
heat
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CN107726672A (en
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公茂琼
郭浩
陈高飞
鹿丁
董学强
徐清宇
沈俊
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Technical Institute of Physics and Chemistry of CAS
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Technical Institute of Physics and Chemistry of CAS
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B33/00—Boilers; Analysers; Rectifiers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B15/00—Sorption machines, plants or systems, operating continuously, e.g. absorption type
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A30/00—Adapting or protecting infrastructure or their operation
    • Y02A30/27—Relating to heating, ventilation or air conditioning [HVAC] technologies
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
    • Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
    • Y02B30/62—Absorption based systems
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Power Engineering (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)

Abstract

The invention relates to energy chemical engineering, and provides a premixed continuous variable temperature distillation generator, which comprises a shell, a first heat exchange pipe and a liquid spraying pipe, wherein the shell is provided with a high-pressure concentrated solution inlet, a first heat source inlet and a first heat source outlet, the shell is also provided with a high-pressure steam outlet and a dilute solution outlet, the outer side of the shell is provided with a premixing unit, and the premixing unit is provided with a dilute solution inlet, a low-pressure absorbed steam inlet and a low-pressure mixed flow outlet; an absorption cycle system is also provided, comprising the generator. The generator can realize the high matching of the solution generation process and the variable-temperature heat source, which shows that the same variable-temperature heat source can realize higher equivalent generation temperature, thereby greatly improving the system efficiency, and the system hardware structure is compact, so that the generator with premixing can not only realize better generation efficiency than the multiple-effect generation in the traditional sense, but also ensure that the system flow organization is more flexible and simple.

Description

Premixing continuous variable temperature distillation generator and absorption type circulating system
Technical Field
The invention relates to the field of energy and chemical engineering, in particular to a premixing continuous variable temperature distillation generator and an absorption type circulating system.
Background
The absorption cycle system is widely applied to the technical fields of refrigeration, power and gas separation and the like, such as an absorption refrigerator/heat pump, an absorption engine (a part of the power cycle system using ammonia-water as a working medium is also commonly called a Kalina cycle engine) and various absorption gas separation systems. These systems all use heat energy as driving force, only consume a small amount of mechanical work, thereby realizing continuous output of refrigerating output and mechanical work (electric energy) or realizing separation of gas components in the process. The basic principle of absorption cycle systems is to separate a concentrated solution into a high-concentration vapor and a low-concentration solution by using heat energy to drive a generation (distillation) process. The steam part enters a subsequent refrigeration (refrigerator/heat pump), a power (engine) subsystem or a gas separation subsystem and the like to realize the output of external useful work or the separation of gas components. The low-concentration solution and the concentrated solution returned from the generator are heated back and then enter the generator, absorb corresponding components again, are converted into the concentrated solution, and then are pressurized again and pumped into the generator to complete a cycle.
The generator of the conventional absorption cycle system, whether with rectification or not, is essentially driven by a constant temperature heat source, i.e. the distillation process inside the generator takes place at a certain fixed temperature (also called the generation temperature). Obviously, in such a generation process, the system has the highest energy utilization efficiency only when the heat source is also a constant-temperature heat source and the temperature is high enough, otherwise, the heat energy utilization quality in the conversion process is reduced. In reality, almost all heat sources with heat energy-temperature distribution characteristics, or temperature-variable heat sources, can be really utilized by energy conversion systems. Therefore, the traditional absorption system generator based on constant temperature distillation driving can not realize good matching with the variable temperature heat source with common practical significance.
In order to fully utilize the variable temperature heat source, the prior research firstly focuses on the technical scheme of utilizing a multistage absorption system, and the process improves the effective utilization problem of the wide variable temperature heat source to a certain extent. However, this solution does not really solve the matching problem of the absorption system with the temperature-changing heat source, and also increases the complexity of the system. In recent years. Many scholars have conducted more research and exploration on the absorption type system, and have proposed the flow of the multiple-effect absorption and non-integral-effect absorption type system, so as to reduce the complexity of the system while improving the system efficiency. The flow of the system is only an improvement of the multi-stage scheme, and the matching problem of the absorption system and the temperature-changing heat source is not solved. Taking a heat source-driven absorption refrigeration system with a wide temperature variation range as an example, the absorption refrigeration system is limited by the effective working temperature area and the efficiency variation characteristics of each stage of absorption system: if a multistage absorption type refrigeration process is adopted, the heat energy of the variable-temperature heat source can be fully utilized, and the cold energy at lower temperature can be prepared. However, if the total temperature span of the heat source is less than the sum of the high-efficiency working temperature spans of all stages, the efficiency of the system is rapidly reduced along with the reduction of the temperature span, and the system is relatively complex. In recent years, many scholars have proposed many new processes for different heat source conditions, for example, for the case that the temperature of the heat source is lower than a certain value, the traditional single-effect absorption refrigerator can not work normally, and as represented by the literature (integrated absorption cycle by indirect thermal sources below 100 ℃ (int.j. energy res.2000; 24: 633-one 640)), a non-integral-effect absorption refrigeration process called 0.x effect is proposed, which has the similar performance to the traditional multistage absorption refrigeration process, but the structure is relatively simple; aiming at the situation that the heat source temperature (highest temperature) is higher than the optimal heat source temperature required by the traditional single-effect absorption type refrigeration process, 1.x effect, double effect and multiple effect concept processes (int.J. Refrig, 1997,20 (2): 120-135) and patent ZL201010104713.4 are proposed. Due to the complexity of the system, the cost and other factors, the application of the three-effect and the more than three-effect process is limited. At present, the main industrial application processes of single-effect, double-effect and 1. x-effect absorption refrigeration are obtained, and particularly the 1. x-effect and 0. x-effect processes are important progresses in the utilization of variable-temperature heat sources, so that the system complexity is taken into consideration, and the system performance is improved. In addition. Patent ZL 2002110664.9 also proposes a self-cascade absorption refrigeration process, which can not only produce the refrigeration capacity with lower temperature than the traditional single-effect absorption refrigeration process, but also has a simpler structure than the multi-stage absorption refrigeration process.
In summary, the conventional absorption systems are essentially based on constant temperature distillation, and although the non-integral 0. x-effect and 1. x-effect absorption systems are improved, they do not fundamentally depart from the concept of constant temperature distillation and increase the complexity of the systems to a certain extent. In general, none of the above systems can be well matched to practical variable temperature heat sources over a wide temperature range.
Disclosure of Invention
The invention aims to provide a continuous variable temperature distillation generator capable of premixing, and aims to solve the problem that the existing absorption system is difficult to realize high matching between a solution generation process and a variable temperature heat source.
The invention is realized by the following steps:
the embodiment of the invention provides a premixed continuous variable temperature distillation generator, which comprises a shell with a cavity, a first heat exchange pipe and a liquid spraying pipe, wherein the first heat exchange pipe and the liquid spraying pipe are positioned in the cavity, the shell is provided with a high-pressure concentrated solution inlet, a first heat source inlet and a first heat source outlet, two ends of the first heat exchange pipe are respectively connected with the first heat source inlet and the first heat source outlet, the liquid spraying pipe is connected with the high-pressure concentrated solution inlet, the shell is also provided with a high-pressure steam outlet and a dilute solution outlet, the liquid spraying pipe is positioned above the first heat exchange pipe, the high-pressure steam outlet and the dilute solution outlet are respectively positioned at the upper side and the lower side of the liquid spraying pipe, the outer side of the shell is provided with a premixing unit, and the premixing unit is provided with a dilute solution inlet, a low-pressure absorbed steam inlet and a low-pressure mixed outflow port, wherein the dilute solution inlet is in communication with the dilute solution outlet.
The embodiment of the invention also provides an absorption type circulating system which comprises a refrigerating device and at least one generator, wherein the first heat exchange tube of each generator and the heating device form a circulating flow path.
The invention has the following beneficial effects:
the generator can realize the high matching of the solution generating process and the variable temperature heat source, and the higher equivalent generating temperature can be realized by the same variable temperature heat source, so that the system efficiency is greatly improved, the system hardware structure is compact, and the premixed continuous variable temperature distillation generator can realize the generating efficiency which is better than the multi-effect generation in the traditional sense and ensure that the system flow organization is more flexible and simple.
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 description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
FIG. 1 is a schematic diagram of embodiment 1 of a premixer-able CVT generator according to the present invention;
FIG. 2 is a schematic diagram of a premixer-able CVT generator in form 2 according to an embodiment of the present invention;
FIG. 3 is a schematic diagram of a type 3 continuous variable temperature distillation generator which can be premixed according to an embodiment of the present invention;
FIG. 4 is a schematic diagram of a form 4 of a premixer-able CVT generator according to an embodiment of the present invention;
FIG. 5 is a schematic diagram of a type 5 continuous variable temperature distillation generator which can be premixed according to an embodiment of the present invention;
FIG. 6 is a schematic diagram of a form 6 of a premixer-able CVT generator according to an embodiment of the present invention;
FIG. 7 is a schematic diagram of a form 7 of a premixer-able CVT generator according to an embodiment of the present invention;
FIG. 8 is a schematic diagram of a form 8 of a premixer-able CVT generator according to an embodiment of the present invention;
FIG. 9 is a schematic diagram of a 9 th embodiment of a premixer-able CVT generator according to an embodiment of the present invention;
FIG. 10 is a schematic diagram of a 10 th embodiment of a premixer able CVT generator according to an embodiment of the present invention;
FIG. 11 is a schematic diagram of a 11 th embodiment of a premixer able CVT generator according to an embodiment of the present invention;
FIG. 12 is a schematic diagram of a premix continuous temperature swing distillation generator of form 12 according to an embodiment of the present invention;
FIG. 13 is a schematic diagram of a 13 th embodiment of a premixer able CVT generator according to an embodiment of the present invention;
FIG. 14 is a schematic diagram of a 14 th embodiment of a premixer able CVT generator according to an embodiment of the present invention;
FIG. 15 is a schematic diagram of form 15 of a premixer able CVT generator according to an embodiment of the present invention;
FIG. 16 is a schematic diagram of a form 16 of a premixer-able CVT generator according to an embodiment of the present invention;
FIG. 17 is a schematic diagram of a 17 th embodiment of a premixer able CVT generator according to an embodiment of the present invention;
FIG. 18 is a schematic diagram of a 18 th embodiment of a premixer able CVT generator according to an embodiment of the present invention;
FIG. 19 is a schematic diagram of a 19 th embodiment of a premixer able CVT generator according to an embodiment of the present invention;
FIG. 20 is a schematic diagram of a 20 th embodiment of a premixer able CVT generator according to an embodiment of the present invention;
FIG. 21 is a schematic diagram of a 21 st version of a premixer able CVT generator according to an embodiment of the present invention;
FIG. 22 is a schematic diagram of a form 22 of a premixer-able CVT generator according to an embodiment of the present invention;
FIG. 23 is a schematic diagram of a 23 rd embodiment of a premixer able CVT generator according to embodiments of the present invention;
FIG. 24 is a schematic diagram of a schematic form 24 of a premixer-able CVT generator according to an embodiment of the present invention;
FIG. 25 is a schematic diagram of form 25 of a premixer able CVT generator according to an embodiment of the present invention;
FIG. 26 is a schematic diagram of a form 26 of a premixer-able CVT generator according to an embodiment of the present invention;
FIG. 27 is a schematic diagram of a form 27 of a premixer-able CVT generator according to an embodiment of the present invention;
FIG. 28 is a schematic diagram of a form 28 of a premixer-able CVT generator according to an embodiment of the present invention;
FIG. 29 is a schematic diagram of a form 29 of a premixer able CVT generator according to an embodiment of the present invention;
FIG. 30 is a schematic diagram of a 30 th embodiment of a premixer-able CVT generator according to an embodiment of the present invention;
FIG. 31 is a schematic diagram of a 31 st version of a premixer able CVT generator according to an embodiment of the present invention;
FIG. 32 is a schematic diagram of a 32 nd version of a premixer able CVT generator according to an embodiment of the present invention;
FIG. 33 is a schematic diagram of a 33 rd version of a premixer able CVT generator according to an embodiment of the present invention;
FIG. 34 is a schematic diagram of a schematic form 34 of a premixer able CVT generator according to an embodiment of the present invention;
FIG. 35 is a schematic diagram of a form 35 of a premixer able CVT generator according to an embodiment of the present invention;
FIG. 36 is a schematic diagram of a 36 th embodiment of a premixer able CVT generator according to an embodiment of the present invention;
FIG. 37 is a schematic diagram of a form 37 of a premixer able CVT generator according to an embodiment of the present invention;
FIG. 38 is a schematic diagram of a form 38 of a premixer able CVT generator according to an embodiment of the present invention;
FIG. 39 is a schematic diagram of an absorption cycle system provided by an embodiment of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Referring to fig. 1, an embodiment of the present invention provides a continuous variable temperature distillation generator capable of premixing, which includes a housing 1 having a chamber, the chamber is a variable temperature distillation space of the generator, the generator further includes a first heat exchange tube 2 and a liquid spray tube 3, the first heat exchange tube 2 and the liquid spray tube 3 are both located in the chamber, the housing 1 is provided with a high pressure concentrated solution inlet, a first heat source inlet and a first heat source heat outlet, two ends of the first heat exchange tube 2 are respectively connected to the first heat source inlet and the first heat source outlet, for which, a heat source can enter the first heat exchange tube 2 from the first heat source inlet, and is discharged from the first heat source outlet after heat exchange through the first heat exchange tube 2, the liquid spray tube 3 is connected to the high pressure concentrated solution inlet, the high pressure concentrated solution enters the liquid spray tube 3 from the high pressure concentrated solution inlet, and is sprayed downward into the chamber from the liquid spray tube 3, the first heat exchange tube 2 is located below the liquid spray tube 3, thereby make 3 below of spray tube for taking place the section, 3 spun high pressure concentrated solution and the heat transfer of first heat exchange tube 2 in the spray tube, high pressure concentrated solution temperature risees, and then produce high-pressure steam and high-pressure dilute solution, wherein high-pressure steam moves to spray tube 3 top, and dilute solution drops downwards under the action of gravity, still be provided with high-pressure steam outlet and dilute solution export on casing 1, and high-pressure steam outlet and dilute solution export are located the upper and lower both sides of spray tube 3 respectively, then the high-pressure steam that produces among the high pressure concentrated solution heat transfer process is by high-pressure steam outlet discharge cavity, and the dilute solution that produces is by dilute solution outlet discharge cavity. In the invention, the high matching of the solution generation process and the variable temperature heat source can be realized in the generator, which shows that the higher equivalent generation temperature can be realized by the same variable temperature heat source, thereby greatly improving the system efficiency, and the system hardware structure is compact, so that the premixed continuous variable temperature distillation generator not only can realize the generation efficiency which is more excellent than the multi-effect generation in the traditional sense, but also can ensure that the flow organization of the system is more flexible and simple.
With reference to fig. 2, in order to optimize the above embodiment, a pre-mixing unit 4 for reducing the pressure and mixing it with the low-pressure steam (absorbed medium) can be arranged at the dilute solution outlet, said pre-mixing unit 4 having an inlet for dilute solution, an inlet for low-pressure absorbed steam and an outlet for low-pressure mixed steam. The structure and the flow mode are as follows: the high-pressure dilute solution flowing out of the dilute solution outlet enters the premixing unit 4 through the dilute solution inlet, is depressurized and mixed with low-pressure absorbed steam introduced from the low-pressure absorbed steam inlet, and then flows out of the low-pressure mixed flow outlet.
Referring to fig. 3, preferably, the generator further comprises a second heat exchange tube 5, the second heat exchange tube 5 is at least partially located in the cavity, and the second heat exchange tube 5 is communicated with the high-pressure steam outlet, wherein the second heat exchange tube 5 is a part in the cavity and has at least one section of second bending structure, when the second heat exchange tube 5 is only arranged on the upper side or the lower side of the liquid spraying tube 3, the second bending structure is one section, otherwise, when the second heat exchange tube 5 is arranged on both the upper side and the lower side of the liquid spraying tube 3, the second bending structure is two sections and is respectively distributed on the upper side and the lower side of the liquid spraying tube 3, the length of the second heat exchange tube 5 in the cavity can be increased through the second bending structure, and further the heat exchange efficiency of the second heat exchange tube 5. The structure and the flow mode are as follows: the regenerated and separated high-pressure steam flows out of the high-pressure steam outlet, enters the second heat exchange tube 5, enters the cavity through the second heat exchange tube 5, and is guided out of the cavity through the second heat exchange tube 5 after heat exchange or heat regeneration along the way; inside the generator, there is formed a continuous temperature-varying distillation section with heat source and regenerated and separated high pressure steam as inner heat transfer flow channel.
Referring to fig. 4, preferably, the generator further comprises a third heat exchange tube 6, at least a part of the third heat exchange tube 6 is located in the cavity, and the third heat exchange tube 6 is communicated with the dilute solution outlet, wherein the third heat exchange tube 6 is a part in the cavity and has at least one section of first bending structure, when the third heat exchange tube 6 is only arranged on the upper side or the lower side of the liquid spraying tube 3, the first bending structure is one section, otherwise, when the third heat exchange tube 6 is arranged on the upper side or the lower side of the liquid spraying tube 3, the first bending structure is two sections and is respectively distributed on the upper side and the lower side of the liquid spraying tube 3, the length of the third heat exchange tube 6 in the cavity can be increased by the first and second bending structures, and the heat exchange efficiency of the third heat exchange tube 6. The structure and the flow mode are as follows: the regenerated and separated high-pressure dilute solution flows out of the dilute solution outlet, enters the third heat exchange tube 6, enters the chamber through the third heat exchange tube 6, is subjected to on-way heat exchange or heat regeneration, and is led out of the chamber through the third heat exchange tube 6; inside the generator, there is formed a continuous temperature-varying distillation section with heat source and regenerated and separated high-pressure dilute solution as internal heat transfer flow channel.
Referring to fig. 5, the generator preferably comprises the second heat exchange tube 5 described above and the third heat exchange tube 6 described above. The structure and the flow mode are as follows: the regenerated and separated high-pressure steam flows out through the high-pressure steam outlet, enters the second heat exchange tube 5, enters the chamber through the second heat exchange tube 5, and is guided out of the chamber through the second heat exchange tube 5 after on-way heat exchange or heat regeneration; the regenerated and separated high-pressure dilute solution flows out of the dilute solution outlet, enters the third heat exchange tube 6, enters the chamber through the third heat exchange tube 6, is subjected to on-way heat exchange or heat regeneration, and is led out of the chamber through the third heat exchange tube 6; inside the generator, there is formed a continuous temperature-varying distillation section with heat source, regenerated and separated high pressure steam and high pressure dilute solution as inner heat transfer flow channel.
Referring to fig. 6, the third heat exchange pipe 6 described above is preferably combined with the premixing unit 4 described above, and the third heat exchange pipe 6 is communicated with the low-pressure mixed stream outlet of the premixing unit 4. The structure and the flow mode are as follows: the high-pressure dilute solution flowing out of the dilute solution outlet enters the premixing unit 4 through the dilute solution inlet, is subjected to pressure reduction and is mixed with low-pressure absorbed steam introduced from the low-pressure absorbed steam inlet, then is introduced into the third heat exchange tube 6 through the low-pressure mixed flow outlet, enters the cavity through the third heat exchange tube 6, and is led out of the cavity through the third heat exchange tube 6 after heat exchange or heat regeneration along the way.
Referring to fig. 7, the above-described premixing unit 4, the second heat exchanging pipe 5 and the third heat exchanging pipe 6 are preferably combined. The structure and the flow mode are as follows: the regenerated and separated high-pressure steam flows out of the high-pressure steam outlet, enters the second heat exchange tube 5, enters the cavity through the second heat exchange tube 5, and is guided out of the cavity through the second heat exchange tube 5 after heat exchange or heat regeneration along the way; the regenerated and separated high-pressure dilute solution flows out of the dilute solution outlet and then enters the premixing unit 4, is subjected to pressure reduction and is mixed with low-pressure absorbed steam introduced from the low-pressure absorbed steam inlet, then is guided into the third heat exchange tube 6 through the low-pressure mixed flow outlet, enters the chamber through the third heat exchange tube 6, and is guided out of the chamber through the third heat exchange tube 6 after heat exchange or heat regeneration along the way.
Referring to fig. 8, preferably, the generator further comprises a cooling pipe 7, a cooling inlet and a cooling outlet are further provided on the housing 1, both ends of the cooling pipe 7 are connected to the cooling inlet and the cooling outlet, respectively, the liquid spray pipe 3 is installed at a middle position of the chamber, the cooling pipe 7 is installed above the liquid spray pipe 3, and a rectification packing section 8 is provided between the cooling pipe 7 and the liquid spray pipe 3, for rectifying or recuperating the high-pressure steam coming from the generation section, the cooling tube 7 has a third bent structure, wherein the third bending structure may be arranged according to the presence or absence of the rectifying packing section 8, for example, when there is no rectifying packing section 8, the third bending structure may extend in a vertical direction, when the rectification packing section 8 is arranged, the third bending structure extends along the horizontal direction, and the heat exchange length of the cooling pipe 7 can be increased through the third bending structure, so that the heat exchange efficiency of the cooling pipe is ensured. The structure and the flow mode are as follows: the cold source enters from the cooling inlet and flows out from the cooling outlet; the high-pressure steam discharged from the generation section flows out from the high-pressure steam outlet after being further separated by the rectification section.
Referring to fig. 9, the cooling tube 7, the rectification packing section 8 and the second heat exchange tube 5 described above are preferably combined. The structure and the flow mode are as follows: the cold source enters from the cooling inlet and flows out from the cooling outlet; the high-pressure steam discharged from the generation section is further separated by the rectification section, flows out from the high-pressure steam outlet, enters the second heat exchange tube 5, enters the cavity through the second heat exchange tube 5, and is guided out of the cavity through the second heat exchange tube 5 after heat exchange or heat regeneration along the way.
Referring to fig. 10, the cooling tubes 7, the rectification packing section 8 and the third heat exchange tubes 6 described above are preferably combined. The structure and the flow mode are as follows: the cold source enters from the cooling inlet and flows out from the cooling outlet; the regenerated and separated high-pressure dilute solution flows out of the dilute solution outlet, enters the third heat exchange tube 6, enters the chamber through the third heat exchange tube 6, is subjected to on-way heat exchange or heat regeneration, and is led out of the chamber through the third heat exchange tube 6; inside the generator, there is formed a continuous temperature-varying distillation section with heat source, regenerated and separated high pressure steam and high pressure dilute solution as inner heat transfer flow channel.
Referring to fig. 11, the above-described cooling tube 7, rectifying packing section 8, second heat exchange tube 5 and third heat exchange tube 6 are preferably combined. The structure and the flow mode are as follows: the cold source enters from the cooling inlet and flows out from the cooling outlet; the high-pressure steam discharged from the generation section is further separated by the rectification section, flows out from a high-pressure steam outlet, enters the second heat exchange tube 5, enters the cavity through the second heat exchange tube 5, and is guided out of the cavity through the second heat exchange tube 5 after passing heat exchange or heat regeneration; the regenerated and separated high-pressure dilute solution flows out of the dilute solution outlet, enters the third heat exchange tube 6, enters the chamber through the third heat exchange tube 6, is subjected to on-way heat exchange or heat regeneration, and is led out of the chamber through the third heat exchange tube 6; inside the generator, there is formed a continuous temperature-varying distillation section with heat source, regenerated and separated high pressure steam and high pressure dilute solution as inner heat transfer flow channel.
Referring to fig. 12, the cooling tubes 7, the rectification packing section 8, the pre-mixing unit 4, and the third heat exchange tubes 6 described above are preferably combined. The structure and the flow mode are as follows: the cold source enters from the cooling inlet and flows out from the cooling outlet; the high-pressure steam discharged from the generation section flows out from a high-pressure steam outlet after being further separated by the rectification section; the high-pressure dilute solution flowing out of the dilute solution outlet enters the premixing unit 4 through the dilute solution inlet, is subjected to pressure reduction and is mixed with low-pressure absorbed steam introduced from the low-pressure absorbed steam inlet, then is introduced into the third heat exchange tube 6 through the low-pressure mixed flow outlet, enters the cavity through the third heat exchange tube 6, and is led out of the cavity through the third heat exchange tube 6 after heat exchange or heat regeneration along the way.
Referring to fig. 13, the cooling tube 7, the rectification packing section 8, the pre-mixing unit 4, the second heat exchange tube 5 and the third heat exchange tube 6 described above are preferably combined. The structure and the flow mode are as follows: the cold source enters from the cooling inlet and flows out from the cooling outlet; the high-pressure steam discharged from the generation section is further separated by the rectification section, flows out from a high-pressure steam outlet, enters the second heat exchange tube 5, enters the cavity through the second heat exchange tube 5, and is guided out of the cavity through the second heat exchange tube 5 after passing heat exchange or heat regeneration; the high-pressure dilute solution flowing out of the dilute solution outlet enters the premixing unit 4 through the dilute solution inlet, is subjected to pressure reduction and is mixed with low-pressure absorbed steam introduced from the low-pressure absorbed steam inlet, then is introduced into the third heat exchange tube 6 through the low-pressure mixed flow outlet, enters the cavity through the third heat exchange tube 6, and is led out of the cavity through the third heat exchange tube 6 after heat exchange or heat regeneration along the way.
Referring to fig. 14, it is preferable that when only the cooling pipe 7 is provided, wherein the cooling pipe 7 is vertically provided. The structure and the flow mode are as follows: the cold source enters from the cooling inlet and flows out from the cooling outlet; the heat source can enter the first heat exchange tube 2 from the first heat source inlet, and is discharged from the first heat source outlet after heat exchange of the first heat exchange tube 2.
Referring to fig. 15, the cooling tube 7 described above is preferably combined with a second heat exchange tube 5, wherein the cooling tube 7 is vertically disposed and the portion of the second heat exchange tube 5 located in the chamber is located below the liquid spray tube 3. The structure and the flow mode are as follows: the cold source enters from the cooling inlet and flows out from the cooling outlet; a heat source can enter the first heat exchange tube 2 from the first heat source inlet, and is discharged from the first heat source outlet after heat exchange of the first heat exchange tube 2; the regenerated and separated high-pressure steam flows out through the high-pressure steam outlet, enters the second heat exchange tube 5, enters the chamber through the second heat exchange tube 5, and is guided out of the chamber through the second heat exchange tube 5 after on-way heat exchange or heat regeneration.
Referring to fig. 16, the cooling pipe 7 is preferably combined with the second heat exchanging pipe 5, wherein the cooling pipe 7 is vertically arranged and the second heat exchanging pipe 5 is distributed on the upper and lower sides of the liquid spray pipe 3. The structure and the flow mode are as follows: the cold source enters from the cooling inlet and flows out from the cooling outlet; a heat source can enter the first heat exchange tube 2 from the first heat source inlet, and is discharged from the first heat source outlet after heat exchange of the first heat exchange tube 2; the regenerated and separated high-pressure steam flows out through the high-pressure steam outlet, enters the second heat exchange tube 5, enters the chamber through the second heat exchange tube 5, and is guided out of the chamber through the second heat exchange tube 5 after on-way heat exchange or heat regeneration.
Referring to fig. 17, the above-described cooling tube 7 is preferably combined with the third heat exchanging tube 6, wherein the cooling tube 7 is vertically disposed. The structure and the flow mode are as follows: the cold source enters from the cooling inlet and flows out from the cooling outlet; the regenerated and separated high-pressure dilute solution flows out of the dilute solution outlet, enters the third heat exchange tube 6, enters the chamber through the third heat exchange tube 6, and is led out of the chamber through the third heat exchange tube 6 after heat exchange or heat regeneration along the way.
Referring to fig. 18, it is preferable to combine the cooling tube 7, the second heat exchanging tube 5 and the third heat exchanging tube 6, wherein the cooling tube 7 is vertically disposed, the portion of the second heat exchanging tube 5 located in the chamber is located above the liquid ejecting tube 3, and the portion of the third heat exchanging tube 6 located in the chamber is located below the liquid ejecting tube 3. The structure and the flow mode are as follows: the cold source enters from the cooling inlet and flows out from the cooling outlet; the high-pressure steam discharged from the generation section flows out of the high-pressure steam outlet, enters the second heat exchange tube 5, enters the cavity through the second heat exchange tube 5, and is guided out of the cavity through the second heat exchange tube 5 after heat exchange or heat regeneration along the way; the regenerated and separated high-pressure dilute solution flows out of the dilute solution outlet, enters the third heat exchange tube 6, enters the chamber through the third heat exchange tube 6, is subjected to on-way heat exchange or heat regeneration, and is led out of the chamber through the third heat exchange tube 6; inside the generator, there is formed a continuous temperature-varying distillation section with heat source, regenerated and separated high pressure steam and high pressure dilute solution as inner heat transfer flow channel.
Referring to fig. 19, the cooling tube 7, the second heat exchanging tube 5 and the third heat exchanging tube 6 are preferably combined, wherein the cooling tube 7 is vertically arranged, and the portion of the second heat exchanging tube 5 located in the chamber and the portion of the third heat exchanging tube 6 located in the chamber are both located below the liquid spraying tube 3. The structure and the flow mode are as follows: the cold source enters from the cooling inlet and flows out from the cooling outlet; the high-pressure steam discharged from the generation section flows out of the high-pressure steam outlet, enters the second heat exchange tube 5, enters the cavity through the second heat exchange tube 5, and is guided out of the cavity through the second heat exchange tube 5 after heat exchange or heat regeneration along the way; the regenerated and separated high-pressure dilute solution flows out of the dilute solution outlet, enters the third heat exchange tube 6, enters the chamber through the third heat exchange tube 6, is subjected to on-way heat exchange or heat regeneration, and is led out of the chamber through the third heat exchange tube 6; inside the generator, there is formed a continuous temperature-varying distillation section with heat source, regenerated and separated high pressure steam and high pressure dilute solution as inner heat transfer flow channel.
Referring to fig. 20, it is preferable to combine the cooling tube 7, the second heat exchanging tube 5 and the third heat exchanging tube 6, wherein the cooling tube 7 is vertically disposed, the portion of the second heat exchanging tube 5 located in the chamber is located at the upper and lower sides of the liquid spraying tube 3, and the portion of the third heat exchanging tube 6 located in the chamber is located below the liquid spraying tube 3. The structure and the flow mode are as follows: the cold source enters from the cooling inlet and flows out from the cooling outlet; the high-pressure steam discharged from the generation section flows out of the high-pressure steam outlet, enters the second heat exchange tube 5, enters the cavity through the second heat exchange tube 5, and is guided out of the cavity through the second heat exchange tube 5 after heat exchange or heat regeneration along the way; the regenerated and separated high-pressure dilute solution flows out of the dilute solution outlet, enters the third heat exchange tube 6, enters the chamber through the third heat exchange tube 6, is subjected to on-way heat exchange or heat regeneration, and is led out of the chamber through the third heat exchange tube 6; inside the generator, there is formed a continuous temperature-varying distillation section with heat source, regenerated and separated high pressure steam and high pressure dilute solution as inner heat transfer flow channel.
Referring to fig. 21, the cooling tube 7, the second heat exchanging tube 5 and the third heat exchanging tube 6 are preferably combined, wherein the cooling tube 7 is vertically arranged, and the portion of the second heat exchanging tube 5 located in the chamber and the portion of the third heat exchanging tube 6 located in the chamber are located at the upper and lower sides of the liquid spraying tube 3. The structure and the flow mode are as follows: the cold source enters from the cooling inlet and flows out from the cooling outlet; the high-pressure steam discharged from the generation section flows out of the high-pressure steam outlet, enters the second heat exchange tube 5, enters the cavity through the second heat exchange tube 5, and is guided out of the cavity through the second heat exchange tube 5 after heat exchange or heat regeneration along the way; the regenerated and separated high-pressure dilute solution flows out of the dilute solution outlet, enters the third heat exchange tube 6, enters the chamber through the third heat exchange tube 6, is subjected to on-way heat exchange or heat regeneration, and is led out of the chamber through the third heat exchange tube 6; inside the generator, there is formed a continuous temperature-varying distillation section with heat source, regenerated and separated high pressure steam and high pressure dilute solution as inner heat transfer flow channel.
Referring to fig. 22, the above-described cooling tube 7, the third heat exchanging tube 6, and the premixing unit 4 are preferably combined, wherein the cooling tube 7 is vertically disposed. The structure and the flow mode are as follows: the cold source enters from the cooling inlet and flows out from the cooling outlet; the high-pressure dilute solution flowing out of the dilute solution outlet enters the premixing unit 4 through the dilute solution inlet, is subjected to pressure reduction and is mixed with low-pressure absorbed steam introduced from the low-pressure absorbed steam inlet, then is introduced into the third heat exchange tube 6 through the low-pressure mixed flow outlet, enters the cavity through the third heat exchange tube 6, and is led out of the cavity through the third heat exchange tube 6 after heat exchange or heat regeneration along the way.
Referring to fig. 23, it is preferable to combine the above-described cooling tube 7, the pre-mixing unit 4, the second heat exchanging tube 5, and the third heat exchanging tube 6, wherein the cooling tube 7 is vertically disposed, a portion of the second heat exchanging tube 5 located in the chamber is located above the liquid ejecting tube 3, and a portion of the third heat exchanging tube 6 located in the chamber is located below the liquid ejecting tube 3. The structure and the flow mode are as follows: the cold source enters from the cooling inlet and flows out from the cooling outlet; the high-pressure steam discharged from the generation section flows out of the high-pressure steam outlet, enters the second heat exchange tube 5, enters the cavity through the second heat exchange tube 5, and is guided out of the cavity through the second heat exchange tube 5 after heat exchange or heat regeneration along the way; the high-pressure dilute solution flowing out of the dilute solution outlet enters the premixing unit 4 from the dilute solution inlet, is subjected to pressure reduction and is mixed with low-pressure absorbed steam introduced from the low-pressure absorbed steam inlet, then is introduced into the third heat exchange tube 6 from the low-pressure mixed flow outlet, enters the chamber through the third heat exchange tube 6, and is led out of the chamber through the third heat exchange tube 6 after heat exchange or heat regeneration along the way; inside the generator, there is formed a continuous temperature-varying distillation section with heat source, regenerated and separated high pressure steam and high pressure dilute solution as inner heat transfer flow channel.
Referring to fig. 24, it is preferable to combine the cooling tube 7, the premixing unit 4, the second heat exchanging tube 5 and the third heat exchanging tube 6 as described above, wherein the cooling tube 7 is vertically disposed, and a portion of the second heat exchanging tube 5 located in the chamber and a portion of the third heat exchanging tube 6 located in the chamber are both located below the liquid ejecting tube 3. The structure and the flow mode are as follows: the cold source enters from the cooling inlet and flows out from the cooling outlet; the high-pressure steam discharged from the generation section flows out of the high-pressure steam outlet, enters the second heat exchange tube 5, enters the cavity through the second heat exchange tube 5, and is guided out of the cavity through the second heat exchange tube 5 after heat exchange or heat regeneration along the way; the high-pressure dilute solution flowing out of the dilute solution outlet enters the premixing unit 4 from the dilute solution inlet, is subjected to pressure reduction and is mixed with low-pressure absorbed steam introduced from the low-pressure absorbed steam inlet, then is introduced into the third heat exchange tube 6 from the low-pressure mixed flow outlet, enters the chamber through the third heat exchange tube 6, and is led out of the chamber through the third heat exchange tube 6 after heat exchange or heat regeneration along the way; inside the generator, there is formed a continuous temperature-varying distillation section with heat source, regenerated and separated high pressure steam and high pressure dilute solution as inner heat transfer flow channel.
Referring to fig. 25, it is preferable to combine the above-mentioned cooling tube 7, the premixing unit 4, the second heat exchanging tube 5 and the third heat exchanging tube 6, wherein the cooling tube 7 is vertically arranged, the portion of the second heat exchanging tube 5 located in the chamber is located at the upper and lower sides of the liquid ejecting tube 3, and the portion of the third heat exchanging tube 6 located in the chamber is located below the liquid ejecting tube 3. The structure and the flow mode are as follows: the cold source enters from the cooling inlet and flows out from the cooling outlet; the high-pressure steam discharged from the generation section flows out of the high-pressure steam outlet, enters the second heat exchange tube 5, enters the cavity through the second heat exchange tube 5, and is guided out of the cavity through the second heat exchange tube 5 after heat exchange or heat regeneration along the way; the high-pressure dilute solution flowing out of the dilute solution outlet enters the premixing unit 4 from the dilute solution inlet, is subjected to pressure reduction and is mixed with low-pressure absorbed steam introduced from the low-pressure absorbed steam inlet, then is introduced into the third heat exchange tube 6 from the low-pressure mixed flow outlet, enters the chamber through the third heat exchange tube 6, and is led out of the chamber through the third heat exchange tube 6 after heat exchange or heat regeneration along the way; inside the generator, there is formed a continuous temperature-varying distillation section with heat source, regenerated and separated high pressure steam and high pressure dilute solution as inner heat transfer flow channel.
Referring to fig. 26, the cooling pipe 7, the premixing unit 4, the second heat exchanging pipe 5 and the third heat exchanging pipe 6 are preferably combined, wherein the cooling pipe 7 is vertically arranged, and the portion of the second heat exchanging pipe 5 located in the chamber and the portion of the third heat exchanging pipe 6 located in the chamber are located at the upper and lower sides of the liquid spraying pipe 3. The structure and the flow mode are as follows: the cold source enters from the cooling inlet and flows out from the cooling outlet; the high-pressure steam discharged from the generation section flows out of the high-pressure steam outlet, enters the second heat exchange tube 5, enters the cavity through the second heat exchange tube 5, and is guided out of the cavity through the second heat exchange tube 5 after heat exchange or heat regeneration along the way; the high-pressure dilute solution flowing out of the dilute solution outlet enters the premixing unit 4 from the dilute solution inlet, is subjected to pressure reduction and is mixed with low-pressure absorbed steam introduced from the low-pressure absorbed steam inlet, then is introduced into the third heat exchange tube 6 from the low-pressure mixed flow outlet, enters the chamber through the third heat exchange tube 6, and is led out of the chamber through the third heat exchange tube 6 after heat exchange or heat regeneration along the way; inside the generator, there is formed a continuous temperature-varying distillation section with heat source, regenerated and separated high pressure steam and high pressure dilute solution as inner heat transfer flow channel.
Referring to fig. 27, preferably, the generator further includes a liquid inlet pipe 9, the liquid inlet pipe 9 communicates the high-pressure concentrated solution inlet with the liquid spraying pipe 3, a fourth bending structure is disposed on the liquid inlet pipe 9, the fourth bending structure is integrally located above the liquid spraying pipe 3, the fourth bending structure can horizontally extend or vertically extend, the length of the liquid inlet pipe 9 in the chamber can be increased, the heat exchange efficiency of the liquid inlet pipe 9 is also improved to a certain extent, and in combination with the third heat exchange pipe 6, the portion of the third heat exchange pipe 6 located in the chamber is located above the liquid spraying pipe 3. The structure and the flow mode are as follows: the high-pressure concentrated solution enters the liquid inlet pipe 9, flows through the rectification section, is directly sprayed after heat exchange or heat regeneration along the way, or further enters the generation section after being sprayed out from the liquid spraying pipe 3; the high-pressure dilute solution flowing out of the dilute solution outlet is led into the third heat exchange tube 6, enters the chamber through the third heat exchange tube 6, and is led out of the chamber through the third heat exchange tube 6 after heat exchange or heat regeneration along the way; inside the generator, there is formed a continuous temperature-varying distillation section with heat source, regenerated and separated high pressure steam and high pressure dilute solution as inner heat transfer flow channel.
Referring to fig. 28, preferably, in combination with the above-mentioned liquid inlet pipe 9 and the third heat exchange pipe 6, the portion of the third heat exchange pipe 6 located in the chamber is distributed on the upper and lower sides of the liquid spray pipe 3. The structure and the flow mode are as follows: the high-pressure concentrated solution enters the liquid inlet pipe 9, flows through the rectification section, is directly sprayed after heat exchange or heat regeneration along the way, or further enters the generation section after being sprayed out from the liquid spraying pipe 3; the high-pressure dilute solution flowing out of the dilute solution outlet is led into the third heat exchange tube 6, enters the chamber through the third heat exchange tube 6, and is led out of the chamber through the third heat exchange tube 6 after heat exchange or heat regeneration along the way; inside the generator, there is formed a continuous temperature-varying distillation section with heat source, regenerated and separated high pressure steam and high pressure dilute solution as inner heat transfer flow channel.
Referring to fig. 29, preferably, in combination with the liquid inlet pipe 9, the second heat exchange pipe 5 and the third heat exchange pipe 6, the part of the second heat exchange pipe 5 located in the chamber is distributed on the lower side of the liquid spraying pipe 3, and the part of the third heat exchange pipe 6 located in the chamber is distributed on the upper side of the liquid spraying pipe 3. The structure and the flow mode are as follows: the high-pressure concentrated solution enters the liquid inlet pipe 9, flows through the rectification section, is directly sprayed after heat exchange or heat regeneration along the way, or further enters the generation section after being sprayed out from the liquid spraying pipe 3; the high-pressure steam discharged from the generation section flows out of the high-pressure steam outlet, enters the second heat exchange tube 5, enters the cavity through the second heat exchange tube 5, and is guided out of the cavity through the second heat exchange tube 5 after heat exchange or heat regeneration along the way; the regenerated and separated high-pressure dilute solution flows out of the dilute solution outlet, enters the third heat exchange tube 6, enters the chamber through the third heat exchange tube 6, is subjected to on-way heat exchange or heat regeneration, and is led out of the chamber through the third heat exchange tube 6; inside the generator, there is formed a continuous temperature-varying distillation section with heat source, regenerated and separated high pressure steam and high pressure dilute solution as inner heat transfer flow channel.
Referring to fig. 30, preferably, in combination with the liquid inlet pipe 9, the second heat exchange pipe 5 and the third heat exchange pipe 6, the part of the second heat exchange pipe 5 located in the chamber is distributed on the upper and lower sides of the liquid spraying pipe 3, and the part of the third heat exchange pipe 6 located in the chamber is distributed on the upper side of the liquid spraying pipe 3. The structure and the flow mode are as follows: the high-pressure concentrated solution enters the liquid inlet pipe 9, flows through the rectification section, is directly sprayed after heat exchange or heat regeneration along the way, or further enters the generation section after being sprayed out from the liquid spraying pipe 3; the high-pressure steam discharged from the generation section flows out of the high-pressure steam outlet, enters the second heat exchange tube 5, enters the cavity through the second heat exchange tube 5, and is guided out of the cavity through the second heat exchange tube 5 after heat exchange or heat regeneration along the way; the regenerated and separated high-pressure dilute solution flows out of the dilute solution outlet, enters the third heat exchange tube 6, enters the chamber through the third heat exchange tube 6, is subjected to on-way heat exchange or heat regeneration, and is led out of the chamber through the third heat exchange tube 6; inside the generator, there is formed a continuous temperature-varying distillation section with heat source, regenerated and separated high pressure steam and high pressure dilute solution as inner heat transfer flow channel.
Referring to fig. 31, preferably, in combination with the liquid inlet pipe 9, the second heat exchange pipe 5 and the third heat exchange pipe 6, the part of the second heat exchange pipe 5 located in the chamber is distributed on the upper and lower sides of the liquid spraying pipe 3, and the part of the third heat exchange pipe 6 located in the chamber is distributed on the upper and lower sides of the liquid spraying pipe 3. The structure and the flow mode are as follows: the high-pressure concentrated solution enters the liquid inlet pipe 9, flows through the rectification section, is directly sprayed after heat exchange or heat regeneration along the way, or further enters the generation section after being sprayed out from the liquid spraying pipe 3; the high-pressure steam discharged from the generation section flows out of the high-pressure steam outlet, enters the second heat exchange tube 5, enters the cavity through the second heat exchange tube 5, and is guided out of the cavity through the second heat exchange tube 5 after heat exchange or heat regeneration along the way; the regenerated and separated high-pressure dilute solution flows out of the dilute solution outlet, enters the third heat exchange tube 6, enters the chamber through the third heat exchange tube 6, is subjected to on-way heat exchange or heat regeneration, and is led out of the chamber through the third heat exchange tube 6; inside the generator, there is formed a continuous temperature-varying distillation section with heat source, regenerated and separated high pressure steam and high pressure dilute solution as inner heat transfer flow channel.
Referring to fig. 32, preferably, in combination with the liquid inlet pipe 9, the second heat exchange pipe 5 and the third heat exchange pipe 6, the part of the second heat exchange pipe 5 located in the chamber is distributed on the lower side of the liquid spraying pipe 3, and the part of the third heat exchange pipe 6 located in the chamber is distributed on the upper and lower sides of the liquid spraying pipe 3. The structure and the flow mode are as follows: the high-pressure concentrated solution enters the liquid inlet pipe 9, flows through the rectification section, is directly sprayed after heat exchange or heat regeneration along the way, or further enters the generation section after being sprayed out from the liquid spraying pipe 3; the high-pressure steam discharged from the generation section flows out of the high-pressure steam outlet, enters the second heat exchange tube 5, enters the cavity through the second heat exchange tube 5, and is guided out of the cavity through the second heat exchange tube 5 after heat exchange or heat regeneration along the way; the regenerated and separated high-pressure dilute solution flows out of the dilute solution outlet, enters the third heat exchange tube 6, enters the chamber through the third heat exchange tube 6, is subjected to on-way heat exchange or heat regeneration, and is led out of the chamber through the third heat exchange tube 6; inside the generator, there is formed a continuous temperature-varying distillation section with heat source, regenerated and separated high pressure steam and high pressure dilute solution as inner heat transfer flow channel.
Referring to fig. 33, it is preferable to combine the above-mentioned liquid inlet pipe 9, third heat exchange pipe 6 and premixing unit 4, wherein the portion of the third heat exchange pipe 6 located inside the chamber is located at the upper side of the liquid spray pipe 3. The structure and the flow mode are as follows: the high-pressure concentrated solution enters the liquid inlet pipe 9, flows through the rectification section, is directly sprayed after heat exchange or heat regeneration along the way, or further enters the generation section after being sprayed out from the liquid spraying pipe 3; the high-pressure dilute solution flowing out of the dilute solution outlet enters the premixing unit 4 through the dilute solution inlet, is subjected to pressure reduction and is mixed with low-pressure absorbed steam introduced from the low-pressure absorbed steam inlet, then is introduced into the third heat exchange tube 6 through the low-pressure mixed flow outlet, enters the cavity through the third heat exchange tube 6, and is led out of the cavity through the third heat exchange tube 6 after heat exchange or heat regeneration along the way.
Referring to fig. 34, it is preferable to combine the above-mentioned liquid inlet pipe 9, third heat exchange pipe 6 and premixing unit 4, wherein the portion of the third heat exchange pipe 6 located in the chamber is located at the upper and lower sides of the liquid spray pipe 3. The structure and the flow mode are as follows: the high-pressure concentrated solution enters the liquid inlet pipe 9, flows through the rectification section, is directly sprayed after heat exchange or heat regeneration along the way, or further enters the generation section after being sprayed out from the liquid spraying pipe 3; the high-pressure dilute solution flowing out of the dilute solution outlet enters the premixing unit 4 through the dilute solution inlet, is subjected to pressure reduction and is mixed with low-pressure absorbed steam introduced from the low-pressure absorbed steam inlet, then is introduced into the third heat exchange tube 6 through the low-pressure mixed flow outlet, enters the cavity through the third heat exchange tube 6, and is led out of the cavity through the third heat exchange tube 6 after heat exchange or heat regeneration along the way.
Referring to fig. 35, it is preferable to combine the above-mentioned liquid inlet pipe 9, second heat exchange pipe 5, third heat exchange pipe 6 and premixing unit 4, wherein the portion of the second heat exchange pipe 5 located in the chamber is located at the lower side of the spray pipe 3, and the portion of the third heat exchange pipe 6 located in the chamber is located at the upper side of the spray pipe 3. The structure and the flow mode are as follows: the high-pressure concentrated solution enters the liquid inlet pipe 9, flows through the rectification section, is directly sprayed after heat exchange or heat regeneration along the way, or further enters the generation section after being sprayed out from the liquid spraying pipe 3; the regenerated and separated high-pressure steam flows out of the high-pressure steam outlet, enters the second heat exchange tube 5, enters the cavity through the second heat exchange tube 5, and is guided out of the cavity through the second heat exchange tube 5 after heat exchange or heat regeneration along the way; the regenerated and separated high-pressure dilute solution flows out of the dilute solution outlet and then enters the premixing unit 4, is subjected to pressure reduction and is mixed with low-pressure absorbed steam introduced from the low-pressure absorbed steam inlet, then is guided into the third heat exchange tube 6 through the low-pressure mixed flow outlet, enters the chamber through the third heat exchange tube 6, and is guided out of the chamber through the third heat exchange tube 6 after heat exchange or heat regeneration along the way.
Referring to fig. 36, it is preferable to combine the above-mentioned liquid inlet pipe 9, second heat exchanging pipe 5, third heat exchanging pipe 6 and premixing unit 4, wherein the portion of the second heat exchanging pipe 5 located in the chamber is located at the upper and lower sides of the spray pipe 3, and the portion of the third heat exchanging pipe 6 located in the chamber is located at the upper side of the spray pipe 3. The structure and the flow mode are as follows: the high-pressure concentrated solution enters the liquid inlet pipe 9, flows through the rectification section, is directly sprayed after heat exchange or heat regeneration along the way, or further enters the generation section after being sprayed out from the liquid spraying pipe 3; the regenerated and separated high-pressure steam flows out of the high-pressure steam outlet, enters the second heat exchange tube 5, enters the cavity through the second heat exchange tube 5, and is guided out of the cavity through the second heat exchange tube 5 after heat exchange or heat regeneration along the way; the regenerated and separated high-pressure dilute solution flows out of the dilute solution outlet and then enters the premixing unit 4, is subjected to pressure reduction and is mixed with low-pressure absorbed steam introduced from the low-pressure absorbed steam inlet, then is guided into the third heat exchange tube 6 through the low-pressure mixed flow outlet, enters the chamber through the third heat exchange tube 6, and is guided out of the chamber through the third heat exchange tube 6 after heat exchange or heat regeneration along the way.
Referring to fig. 37, it is preferable to combine the liquid inlet pipe 9, the second heat exchange pipe 5, the third heat exchange pipe 6 and the premixing unit 4, wherein the portion of the second heat exchange pipe 5 located in the chamber is located at the upper and lower sides of the liquid spray pipe 3, and the portion of the third heat exchange pipe 6 located in the chamber is located at the upper and lower sides of the liquid spray pipe 3. The structure and the flow mode are as follows: the high-pressure concentrated solution enters the liquid inlet pipe 9, flows through the rectification section, is directly sprayed after heat exchange or heat regeneration along the way, or further enters the generation section after being sprayed out from the liquid spraying pipe 3; the regenerated and separated high-pressure steam flows out of the high-pressure steam outlet, enters the second heat exchange tube 5, enters the cavity through the second heat exchange tube 5, and is guided out of the cavity through the second heat exchange tube 5 after heat exchange or heat regeneration along the way; the regenerated and separated high-pressure dilute solution flows out of the dilute solution outlet and then enters the premixing unit 4, is subjected to pressure reduction and is mixed with low-pressure absorbed steam introduced from the low-pressure absorbed steam inlet, then is guided into the third heat exchange tube 6 through the low-pressure mixed flow outlet, enters the chamber through the third heat exchange tube 6, and is guided out of the chamber through the third heat exchange tube 6 after heat exchange or heat regeneration along the way.
Referring to fig. 38, it is preferable to combine the above-mentioned liquid inlet pipe 9, second heat exchanging pipe 5, third heat exchanging pipe 6 and premixing unit 4, wherein the portion of the second heat exchanging pipe 5 located in the chamber is located at the lower side of the spray pipe 3, and the portion of the third heat exchanging pipe 6 located in the chamber is located at the upper and lower sides of the spray pipe 3. The structure and the flow mode are as follows: the high-pressure concentrated solution enters the liquid inlet pipe 9, flows through the rectification section, is directly sprayed after heat exchange or heat regeneration along the way, or further enters the generation section after being sprayed out from the liquid spraying pipe 3; the regenerated and separated high-pressure steam flows out of the high-pressure steam outlet, enters the second heat exchange tube 5, enters the cavity through the second heat exchange tube 5, and is guided out of the cavity through the second heat exchange tube 5 after heat exchange or heat regeneration along the way; the regenerated and separated high-pressure dilute solution flows out of the dilute solution outlet and then enters the premixing unit 4, is subjected to pressure reduction and is mixed with low-pressure absorbed steam introduced from the low-pressure absorbed steam inlet, then is guided into the third heat exchange tube 6 through the low-pressure mixed flow outlet, enters the chamber through the third heat exchange tube 6, and is guided out of the chamber through the third heat exchange tube 6 after heat exchange or heat regeneration along the way.
Referring to fig. 39, an absorption cycle system according to an embodiment of the present invention further includes a refrigeration device Q and at least one generator R, where the cooling pipe 7 of each generator a forms a circulation flow path with the heating device Q. In this embodiment, the refrigeration device Q is used in combination with the generator, and one or more generators R may be used in combination with the refrigeration device Q, where the generators R are connected in parallel, and when the number of the generators R is n, for example, R is n1、R2、R3....Ri...RnThe generators R can be one or more than one of the generators disclosed above, and the absorption efficiency of the generators R is obviously improved through the matching, and the consumption of the cooling medium is greatly reduced, so that the efficiency of the whole absorption type circulating system is completely improved.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the present invention. The invention should not be construed as being limited to the particular embodiments described herein, but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.

Claims (14)

1. A premixerable continuous variable temperature distillation generator, comprising a housing having a chamber, characterized in that: the heat exchanger also comprises a first heat exchange tube and a liquid spraying tube, wherein the first heat exchange tube and the liquid spraying tube are both positioned in the cavity, the shell is provided with a high-pressure concentrated solution inlet, a first heat source inlet and a first heat source outlet, two ends of the first heat exchange tube are respectively connected with the first heat source inlet and the first heat source outlet, the liquid spraying pipe is connected with the high-pressure concentrated solution inlet, the shell is also provided with a high-pressure steam outlet and a dilute solution outlet, the liquid spraying pipe is positioned above the first heat exchange pipe, the high-pressure steam outlet and the dilute solution outlet are respectively positioned at the upper side and the lower side of the liquid spraying pipe, a premixing unit is arranged at the outer side of the shell, the pre-mixing unit has a dilute solution inlet, a low pressure absorbed steam inlet, and a low pressure mixed stream outlet, wherein the dilute solution inlet is in communication with the dilute solution outlet;
the premixing unit is characterized by further comprising a third heat exchange pipe, wherein the third heat exchange pipe is communicated with a low-pressure mixed flow outlet of the premixing unit, and at least part of the third heat exchange pipe is positioned in the cavity;
the part of the third heat exchange tube, which is positioned in the cavity, is positioned above the liquid spraying tube;
or the part of the third heat exchange tube, which is positioned in the cavity, is distributed on the upper side and the lower side of the liquid spraying tube;
the high-pressure steam generator further comprises a second heat exchange tube, the second heat exchange tube is communicated with the high-pressure steam outlet, and at least part of the second heat exchange tube is located in the cavity.
2. The premixerable, continuous variable temperature distillation generator of claim 1, wherein: the part of the third heat exchange tube, which is positioned in the cavity, is provided with at least one section of first bending structure, and the first bending structure extends along the vertical direction.
3. The premixerable, continuous variable temperature distillation generator of claim 1, wherein: the part of the second heat exchange tube, which is positioned in the cavity, is positioned above the liquid spraying tube.
4. The premixerable, continuous variable temperature distillation generator of claim 1, wherein: the part of the second heat exchange tube, which is positioned in the cavity, is positioned below the liquid spraying tube.
5. The premixerable, continuous variable temperature distillation generator of claim 1, wherein: the part of the second heat exchange tube, which is positioned in the cavity, is distributed on the upper side and the lower side of the liquid spraying tube.
6. The premixerable, continuous variable temperature distillation generator of claim 1, wherein: the part of the second heat exchange tube, which is positioned in the cavity, is provided with at least one section of second bending structure, and the second bending structure extends along the vertical direction.
7. The premixerable, continuous variable temperature distillation generator of claim 1, wherein: still including being located cooling tube in the cavity, still be provided with cooling inlet and cooling outlet on the casing, the both ends of cooling tube are connected respectively cooling inlet with the cooling outlet, the cooling tube is located spray tube top.
8. The premixerable, continuous variable temperature distillation generator of claim 7, wherein: the device also comprises a rectification packing section which is positioned between the cooling pipe and the liquid spraying pipe.
9. The premixerable, continuous variable temperature distillation generator of claim 8, wherein: the cooling pipe is provided with a third bending structure, and the third bending structure extends along the horizontal direction.
10. The premixerable, continuous variable temperature distillation generator of claim 1, wherein: the high-pressure steam outlet is positioned at the top end of the shell, and the dilute solution outlet is positioned at the bottom end of the shell.
11. The premixerable, continuous variable temperature distillation generator of claim 1, wherein: still include the feed liquor pipe, the feed liquor pipe intercommunication the high-pressure concentrated solution import with the spray tube, be provided with the fourth structure of buckling on the feed liquor pipe.
12. The premixerable cvt generator of claim 11, wherein: the liquid inlet pipe is positioned above the liquid spraying pipe.
13. The premixerable cvt generator of claim 11, wherein: the fourth bending structure extends along the vertical direction or the horizontal direction.
14. An absorption cycle system, including heating device, its characterized in that: further comprising at least one generator according to any one of claims 1 to 5, said first heat exchange tube of each of said generators forming a circulating flow path with said heating means.
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