CN102269509B - CO2 compression and liquefaction system combined with waste heat driven refrigeration - Google Patents

CO2 compression and liquefaction system combined with waste heat driven refrigeration Download PDF

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CN102269509B
CN102269509B CN201110197232.7A CN201110197232A CN102269509B CN 102269509 B CN102269509 B CN 102269509B CN 201110197232 A CN201110197232 A CN 201110197232A CN 102269509 B CN102269509 B CN 102269509B
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waste heat
evaporimeter
liquid
compressor
compression
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CN102269509A (en
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段立强
陈新明
杨勇平
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North China Electric Power University
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North China Electric Power University
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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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0266—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of carbon dioxide
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/067—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of carbon dioxide
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/02—Compressor intake arrangement, e.g. filtering or cooling
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/04—Compressor cooling arrangement, e.g. inter- or after-stage cooling or condensate removal
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/80—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being carbon dioxide
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/80—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being carbon dioxide
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/02—Integration in an installation for exchanging heat, e.g. for waste heat recovery
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/906—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by heat driven absorption chillers

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Sorption Type Refrigeration Machines (AREA)

Abstract

The invention belongs to the technical field of CO2 post treatment, and in particular relates to a CO2 compression and liquefaction system combined with waste heat driven refrigeration. Based on the CO2 compression and liquefaction system consisting of a multistage compressor, a cooler and a circulating water system, a CO2 gas pre-cooling system, an ammonia absorption type refrigerating system, astaged cooling system, a waste heat steam extraction system, a liquid oxygen pump supercharging system and a liquid CO2 cold reclaiming system are additionally provided; and through the measures of combining the rich waste heat environment of a power plant, making cold by using a waste heat driven refrigerating machine, reducing the liquefaction pressure of CO2 with low temperature and raising the pressure by using the pump after the CO2 is liquefied and the like, the total CO2 compression power consumption is reduced, the electrical energy is saved, and the heat efficiency of the whole plantis improved. The system is suitable for multiple occasions supplied with waste heat and required for compressing and liquefying CO2, and particularly can effectively utilize the waste heat of the power plant and reduce the energy consumption level of CO2 compression and liquefaction in the thermal power plant required for reclaiming the CO2.

Description

Drive the CO that refrigeration combines with waste heat 2Compress and liquefy system
Technical field
The invention belongs to CO 2Post-processing technology field, particularly a kind of CO that combines with waste heat driving refrigeration 2Compress and liquefy system.
Background technology
At present, because dynamical system CO 2The greenhouse effects that discharging causes are more and more serious, thereby, CO 2Catch, seal up for safekeeping and utilize and become the focus of research at present both at home and abroad.The CO that from dynamical system, catches 2Before burying, need to be compressed to 80bar even higher pressure becomes liquid state, be beneficial to long-distance transmissions.Yet this process will expend a large amount of merits.The mode that conventional method adopts plural serial stage to compress step by step usually is with CO 2Gas be compressed to critical pressure with on the CO that liquefies 2, can obtain high pressure and liquid CO simultaneously 2, this is present popular main technological route.The method of this direct compression adopts the intercooled measure of implements spatial scalable compression more, and low-temperature receiver adopts the recirculated cooling water of normal temperature.This method device structure is simple, easy to operate, can realize CO 2Supercharging and liquefaction.But because CO 2Critical pressure very high (reaching 7.38MPa), general compression all is to begin compression from normal pressure (0.1MPa), and pressure ratio is excessive to make that the compressor power consumption is too high, again because use the recirculated water cooling of normal temperature, make that the temperature of suction port of compressor gas is too high, further increased compression power consumption again.This just makes and compresses and liquefies CO 2Total power consumption too high, cause the waste of the energy and the loss of economic benefit.
Summary of the invention
The present invention is for solving conventional compression liquefaction CO 2The problem that the system compresses power consumption is too high has proposed a kind of CO that compresses and liquefies that freezes and combine with the waste heat driving 2System, can reduce compressing and liquefying CO effectively 2The work done during compression of process, total energy consumption also can remain on lower scope.
The technical solution used in the present invention is: the CO that compresses and liquefies that is being made up of compound compressor, cooler, circulation 2Increased CO on the basis of system 2Gas chilldown system, ammonia absorption refrigeration systems, classification cooling system, waste heat steam bleeding system, liquid oxygen pump pressure charging system and liquid CO 2The cold recovery system.
Described CO 2Gas chilldown system and classification cooling system are: before each stage compressor and the CO behind the most end stage compressor 2The evaporimeter of two-stage series connection is set on the pipeline respectively, and the evaporating temperature of previous stage evaporimeter is-15 ℃, and the evaporating temperature of back one-level evaporimeter is-30 ℃.
Described ammonia absorption refrigeration systems is: the outlet of ammonia absorption refrigeration systems is connected with described each evaporimeter, and the cold that uses refrigeration machine to produce comes the CO of cooling compressor entrance 2Gas, and take away CO 2Latent heat during liquefaction; Circulation is as the low-temperature heat source of ammonia absorption refrigerator.
Described waste heat steam bleeding system is: the pump-line that is connected with ammonia absorption refrigeration systems is set, and the Low Temperature Steam that extracts former generating set or other vapour source is used for satisfying ammonia absorption refrigeration systems to the demand of heat energy.
Described liquid oxygen pump pressure charging system and liquid CO 2Cold recovery is: behind final stage evaporimeter, series connection is used for the liquid CO of pressurization 2Liquid oxygen pump, and the heat exchanger that is connected with liquid oxygen pump is set respectively before all evaporators between first order compressor and the most end stage compressor and before the first evaporator behind the most end stage compressor; Liquid oxygen pump is with liquid CO 2Rise to specified pressure, CO 2The liquid regenerators at different levels of flowing through are with the CO before the liquefaction 2Gas carries out heat exchange, reclaims CO 2The cold energy of liquid.
The concrete structure of described ammonia absorption refrigeration systems is: rectifying column, generator, solution heat exchanger, first order absorber, first order solution booster, second level absorber, second level solution booster are connected successively, return rectifying column again after the heat exchange of rework solution heat exchanger then, form minor loop; The ammonia outlet of rectifying column is connected with condenser, is connected respectively to then on the evaporimeters at different levels.
Beneficial effect of the present invention is:
Native system can be finished CO 2When gas compresses and liquefies, increase UTILIZATION OF VESIDUAL HEAT IN, reduce consumption of compressor, reduce the useful work loss, reduce power consumption, make CO 2The total energy consumption that compresses and liquefies reduces, and improves the thermal efficiency of full factory.
Adopt legacy equipment to compress and liquefy CO 2Energy consumption mainly come from the wasted work of compressor, the compressor power consumption is huge, by Motor Drive, consumption be high-quality electric energy.Native system has been introduced ammonia absorption refrigerator.There is being sufficient or low temperature exhaust heat more than needed can support the thermal power plant of utilization or other need compress and liquefy CO 2Occasion, ammonia absorption refrigerator can take full advantage of these waste heats and produce cold and cool off CO 2, consume electric power not.At low temperatures, rise to identical pressure, consumption of compressor can significantly reduce.Again because adopt sub-cooled, make CO 2Saturation pressure reduce, dwindled gaseous state CO 2The scope of boosting, this has further reduced consumption of compressor again.
Description of drawings
Fig. 1 is the structural representation of system of the present invention.
Number in the figure:
The liquid CO of 0- 2Outlet; 1-CO 2The gas access; The 2-first evaporator; 3-second level evaporimeter; 4-first order compressor; The 5-third evaporator; 6-fourth stage evaporimeter; The 7-high stage compressor; 8-level V evaporimeter; The 6th grade of evaporimeter of 9-; 10-third level compressor; The 7th grade of evaporimeter of 11-; The 8th grade of evaporimeter of 12-; The 13-liquid oxygen pump; The 14-condenser; The 15-rectifying column; The 16-generator; The 17-solution heat exchanger; 18-first order absorber; 19-first order solution booster; 20-second level absorber; 21-second level solution booster.
The specific embodiment
The invention provides a kind of CO that combines with waste heat driving refrigeration 2Compress and liquefy system, the present invention will be further described below by description of drawings and the specific embodiment.
Structure chart of the present invention is as shown in Figure 1: CO 2Gas is from CO 2Gas access 1 enters, flow through first evaporator 2 successively, second level evaporimeter 3, first order compressor 4, third evaporator 5, fourth stage evaporimeter 6, high stage compressor 7, level V evaporimeter 8, the 6th grade of evaporimeter 9, third level compressor 10, the 7th grade of evaporimeter 11, the 8th grade of evaporimeter 12 and liquid oxygen pump 13, and then successively through being installed in fourth stage evaporimeter 6, heat exchanger before the third evaporator 5, and be installed in the 6th grade of evaporimeter 9, level V evaporimeter 8, heat exchanger before the 7th grade of evaporimeter 11 will cold energy discharges the back and is flowed out by outlet 0.
The ammonia absorption type refrigerating part of native system is: rectifying column 15, generator 16, solution heat exchanger 17, first order absorber 18, first order solution booster 19, second level absorber 20, second level solution booster 21 are connected successively, return rectifying column 15 again after 17 heat exchange of rework solution heat exchanger then, form minor loop; The ammonia outlet of rectifying column 15 is connected with condenser 14, is connected respectively to then on the evaporimeters at different levels.Employing ammoniacal liquor is cold-producing medium, and two cryogenic temperatures are provided.Evaporating temperature in first evaporator 2, third evaporator 5, level V evaporimeter 8, the 7th grade of evaporimeter 11 is-15 ℃, and the evaporating temperature in second level evaporimeter 3, fourth stage evaporimeter 6, the 6th grade of evaporimeter 9, the 8th grade of evaporimeter 12 is-30 ℃.CO 2Flow through the earlier evaporimeter of higher temperature, the evaporimeter of the lower temperature of flowing through again utilizes the classification cooling, can reduce heat transfer temperature difference, reduces the loss.
The ammonia absorption type refrigerating method of introducing is as follows: ammonia absorption refrigerator adopts low-grade waste heat to drive, not consumed power and mechanical power.Waste heat draws gas and causes generator 16, and the ammonia spirit of heating high concentration produces ammonia; Liquefied ammonia by the high pressure of condenser 14 is divided into stereotyped writing, respectively at four groups of evaporimeters (first evaporator 2 and the second level evaporimeter 3 of connecting in twos, third evaporator 5 and fourth stage evaporimeter 6, level V evaporimeter 8 and the 6th grade of evaporimeter 9, the 7th grade of evaporimeter 11 and the 8th grade of evaporimeter 12) interior evaporation, evaporimeter of each group series connection has-15 ℃ and-30 ℃ of two evaporating temperatures.CO 2Always flow through earlier-15 ℃ evaporimeter ,-30 ℃ the evaporimeter of flowing through again after temperature reduces.
Introduce CO 2Forecooling method as follows: CO 2Original state close to normal temperature and pressure, entering before first order compressor 4 compresses, the preceding double effect evaporator of flowing through successively earlier makes temperature be reduced to-30 ℃ approximately step by step; After each level compression before, all pass through similar cooling, make CO 2Compression remain on low temperature and carry out.
The CO that introduces 2The method of boosting again after the liquefaction is as follows: through sub-cooled, and CO 2Remained on lower temperature, saturation pressure decreases, CO in the 8th grade of evaporimeter 12 2Realized liquefaction, but pressure can not meet the demands still, increase liquid oxygen pump 13, with the CO of liquid state 2Further boost to specified pressure.
The cooling capacity recovering method of introducing is as follows: the liquid CO that liquid oxygen pump 13 comes out 2Temperature is very low, carry a large amount of cold energy, and then successively through being installed in the heat exchanger before the fourth stage evaporimeter 6, third evaporator 5, and be installed in heat exchanger before the 6th grade of evaporimeter 9, level V evaporimeter 8, the 7th grade of evaporimeter 11, the CO of the higher temperature that cooling is come out from each stage compressor 2Gas makes self temperature rising simultaneously, discharges cold energy.
Below in conjunction with actual production, effect of the present invention is done detailed description.
Having chosen initial state in the comparison example is 30 ℃, and pressure is the CO of 0.1MPa 2Gas is research object, it need be compressed to the supercriticality of 8.1MPa.Use the conventional method that compresses and liquefies need use four-stage compressor, every grade of pressure ratio is 3, and compressor efficiency is 0.75, and final total consumption is 358.84kJ/kgCO 2, wherein, only consumption of compressor is just up to 357.56kJ/kgCO 2And native system adopts three grades of gas compressions and the supercharging of one-level liquid oxygen pump, and the work done during compression of consumption is less, and extra ammonia absorption refrigerator only need consume the low-grade heat energy of part.When acting ability higher when the thermodynamic coefficient of refrigeration machine or the inferior heat energy that consumes was very little, the power consumption that this partial heat energy of refrigeration machine additive decrementation is converted into was very little.
The quality of the steam of refrigeration machine consumption is weighed with the folding work factor, i.e. if the middle low temperature heat energy of kind of refrigeration cycle consumption is the power that can export for doing work and the ratio of its heat.Steam quality is more high, and the folding work factor is more big.Can see that from table 1 along with the folding work factor increases, the total energy consumption of native system raises gradually.In addition, the total energy consumption of native system changes to some extent with used steam quality difference: if utilization is the waste heat of discarding originally in the factory, it is zero then rolling over work factor, total the energy consumption of this moment includes only the merit of compressor consumption, only is 183.56kJ/kgCO 2, descend about 48.04% than the conventional method total energy consumption.Usually, the temperature of used heating steam is no more than 165 ℃ in the kind of refrigeration cycle, and roll over work factor accordingly and be not more than 0.1, as can be seen from Table 1, even estimate that by the most conservative situation the total energy consumption of new method still can descend 27.91% than conventional method.
Table 1: the total power consumption when adopting the generator of Steam Heating ammonia absorption refrigerator of different qualities in the native system relatively
Figure BDA0000075846620000061
Be example with the conventional coal-burning power plant of 600MW, suppose that this factory's fuel is Jiaozhuo anthracite, phosphorus content is 66.1%, and low heat valve is 22880kJ/kg.Getting factory's generating efficiency is 40%, and then the electric energy that sends of every burning 1kg coal is 9152kJ, discharges 2.424kgCO simultaneously 2With these CO 2The recovery back transporting and storing for ease of the later stage, it need be compressed to more than the 80bar.Associative operation data in this example see Table 2.
Table 2: the associative operation data among the embodiment
Figure BDA0000075846620000062
Compress and liquefy CO with routine 2The result of method relatively sees Table 3.As can be seen from Table 3, for the CO in thermal power plant 2Compress and liquefy, adopt new method can make generated energy improve one percentage point nearly than conventional method.For the power plant of 600MW, supposing has oepration at full load in 280 days its every year, and every degree electricity price is 0.36 yuan, can increase surplus the benefit 1,600 ten thousand yuan so every year at least.
Table 3: native system and routine compress and liquefy CO 2The result of equipment relatively
Specific energy consumption Energy consumption accounts for generated energy proportion
Conventional equipment 358.84 9.50％
Native system 254.29 6.73％
Drop-out value 104.55 2.77％
Decline percentage 29.14 29.16

Claims (2)

1. drive the CO that refrigeration combines with waste heat 2Compress and liquefy system, it is characterized in that: the CO that compresses and liquefies that is being formed by compound compressor 2Ammonia absorption refrigeration systems, CO have been increased on the basis of system 2Gas chilldown system and classification cooling system, waste heat steam bleeding system, liquid oxygen pump pressure charging system and liquid CO 2The cold recovery system;
Described CO 2Gas chilldown system and classification cooling system are: before each stage compressor and the CO behind the most end stage compressor 2The evaporimeter of two-stage series connection is set on the pipeline respectively, and the evaporating temperature of previous stage evaporimeter is-15 ℃, and the evaporating temperature of back one-level evaporimeter is-30 ℃;
Described ammonia absorption refrigeration systems is: the ammonia absorption refrigerator condensator outlet is connected with described each evaporimeter, and the cold that uses refrigeration machine to produce comes the CO of cooling compressor entrance 2Gas;
Described waste heat steam bleeding system is: the pump-line that is connected with ammonia absorption refrigeration systems is set, and the Low Temperature Steam that extracts former generating set or other vapour source is used for satisfying ammonia absorption refrigeration systems to the demand of heat energy;
Described liquid oxygen pump pressure charging system and liquid CO 2The cold recovery system is: behind final stage evaporimeter, series connection is used for the liquid CO of pressurization 2Liquid oxygen pump, and the heat exchanger that is connected with liquid oxygen pump is set respectively before all evaporators between first order compressor and the most end stage compressor and before the first evaporator behind the most end stage compressor; Liquid oxygen pump is with liquid CO 2Rise to specified pressure, CO 2The liquid heat exchangers at different levels of flowing through are with the CO before the liquefaction 2Gas carries out heat exchange, reclaims CO 2The cold energy of liquid.
2. according to claim 1 and waste heat drive the CO that refrigeration combines 2Compress and liquefy system, it is characterized in that, the concrete structure of described ammonia absorption refrigeration systems is: rectifying column, generator, solution heat exchanger, first order absorber, first order solution booster, second level absorber, second level solution booster are connected successively, return rectifying column again after the heat exchange of rework solution heat exchanger then, form minor loop; The ammonia outlet of rectifying column is connected with condenser, is connected respectively to then on the evaporimeters at different levels.
CN201110197232.7A 2011-07-14 2011-07-14 CO2 compression and liquefaction system combined with waste heat driven refrigeration Expired - Fee Related CN102269509B (en)

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CN103075325B (en) * 2013-02-01 2015-04-15 郑州大学 Compressor waste heat utilization system and compressor inter-stage waste heat utilization system
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