CN104056462B - A kind of heat pump distillation energy saver - Google Patents

A kind of heat pump distillation energy saver Download PDF

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Publication number
CN104056462B
CN104056462B CN201410329144.1A CN201410329144A CN104056462B CN 104056462 B CN104056462 B CN 104056462B CN 201410329144 A CN201410329144 A CN 201410329144A CN 104056462 B CN104056462 B CN 104056462B
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heat exchanger
flash column
destilling tower
connects
compressor
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CN104056462A (en
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任毅
李东林
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CHENGDU HUAXITANG ENVIRONMENT PROTECTION TECHNOLOGY CO., LTD.
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CHENGDU HUAXITANG INVESTMENT Co Ltd
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    • 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
    • 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
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
    • 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
    • Y02P20/50—Improvements relating to the production of bulk chemicals

Abstract

The invention provides a kind of heat pump distillation energy saver, comprise destilling tower, flash column, compressor, liquid outlet bottom described destilling tower connects the inlet of flash column, the exhaust outlet at flash column top connects the air inlet of compressor, the exhaust outlet of compressor connects the air inlet of destilling tower bottom, the exhaust outlet at described destilling tower top is provided with connecting pipe, connecting pipe is provided with heat exchanger, the inlet of this heat exchanger is connected with the liquid outlet of flash column, the liquid outlet of heat exchanger is connected with the inlet on flash column top, the feed pipe of described destilling tower is also provided with heat exchanger, the inlet of this heat exchanger connects the liquid outlet of flash column, the liquid outlet of heat exchanger connects another heat exchanger.The present invention, from the angle reducing plant energy consumption, raising efficiency, simple flow, reduction investment, achieves the application advantage of heat pump at retort field to greatest extent, reduce energy consumption more than 70% compared with conventional distil-lation device.

Description

A kind of heat pump distillation energy saver
Technical field
The present invention relates to heat pump distillation technical field, be specifically related to a kind of heat pump distillation energy saver.
Background technology
Chemical industry is energy consumption rich and influential family, wherein distills and is the high unit operations of energy consumption, and traditional distillation mode thermodynamic efficiency is very low, and energy dissipation is very large.As passed through separated SO in document " application of the rich regenerable amine process desulfur technology of health generation " (" sulfuric acid industry ", 2007 (1): 39 ~ 45) from desulfurization absorbing liquid 2, sweetening liq per ton need consume the saturated vapor of 0.1 ~ 0.2t0.6MPa; From coking ammonia water, pass through the ammonia in separated solution in " ammonia still process new technology is in the application of Shoudu Iron and Steel Co capital Tang engineering " (" fuel and chemical industry ", 2008 (4): 33 ~ 35), remained ammonia per ton needs the saturated vapor of consumption ~ 175Kg0.6MPa; " Gas Purification Factory desulfurizer energy consumption analysis and Discussion on Saving Energy Measures " (" oil gas field environmental protection ", 2013 (5): 20 ~ 25) adopt MEDA de-H from natural gas 2s, CO 2from solution, H in solution is reclaimed afterwards by distillation 2s, CO 2, the document analyzes MDEA method desulfurization energy flow situation, and surplus solution per ton also needs the saturated vapor of consumption 150 ~ 200Kg0.6MPa, propose adopt heat pump compression distillation tower top sour gas after for the lean solution at the bottom of reboiler heating tower.
When today, energy prices rose steadily, how to reduce the energy consumption of destilling tower, make full use of low-temperature heat source, become people's question of common concern.This be there has been proposed to many conservation measures, shown by a large amount of theory analysises, experimental study and commercial Application, wherein energy-saving effect is heat pump distillation technology very significantly.Heat pump techniques is that the energy recovery received much attention in the world in recent years utilizes technology, and it, mainly through consuming a part of mechanical energy, electric energy etc. for compensating, makes the transmission of heat energy realization from low-temperature heat source to high temperature heat source.Because low temperature heat energy can be converted to high temperature heat by heat pump, improving the effective rate of utilization of the energy, is therefore the important channel of reclaiming low temperature exhaust heat.
General employing heat pump distillation heats up overhead steam pressurized, makes it be used as the thermal source of tower bottom reboiler, reclaims the condensation latent heat of overhead vapours.Multiple heat pump distillation flow process is described in document " the heat-pump rectifying process process analysis in energy saving of chemical industry " (" energy-conservation ", 2004 (10): 19 ~ 22).But these flow processs exist significantly not enough when embody rule, major defect is:
1, invest high, technological process is complicated, high concentration poisonous and harmful medium directly adopts compressor compresses, and compressor seriously corroded or material rate require high, and heat recovery is insufficient;
2, the gas after compression is containing incoagulable gas, and cause reboiler heat transfer efficiency low, reboiler duty pressure is high, perishable;
As coking ammonia water distillation uses the problems such as any flow process in above-mentioned document all exists seriously corroded or material rate requires height, blocking, flow process is complicated, recuperation of heat is insufficient.
201110128227.0, name is called the patent of invention of the heat pump regeneration flow process of desulfurization solvent " in the solvent cycle absorption method flue gas desulfurization ", the regeneration gas compressed action that produces during by regenerating desulfurization solvent with compressor, become high-temperature high-pressure overheat steam, and with this superheated steam for thermal source heats regeneration tower bottoms and vaporizes, thus achieve the recycling to tower top low-temp recovery gas waste heat.This flow process overhead gas is containing the SO of high concentration 2, seriously corroded, or to material rate require high, flow process is complicated.
2010101232510, name is called " heat pump flash distillation stripping deamination method ", with 2012101536708, name is called the patent of invention of " a kind of processing method of the strong ammonia wastewater based on both vapor compression ", two kinds of methods all need to use reboiler, and technological process is complicated, still there is compressor and contacts with high concentration ammonia, seriously corroded, or material rate requires high problem.
Summary of the invention
The present invention, in order to reduce plant energy consumption and the simple flow of heat pump distillation, provides a kind of heat pump distillation energy saver, is specially adapted to adopt the situation of distilling solution.The present invention is from the angle reducing plant energy consumption, raising efficiency, simple flow, reduction investment, achieve the application advantage of heat pump at retort field to greatest extent, heat pump techniques is combined with distillation, forms that adapt with distillation, that technological process is simple, small investment, energy-saving efficiency are high heat pump distillation energy saver.
For achieving the above object, the present invention adopts following technical scheme:
A kind of heat pump distillation energy saver, it is characterized in that: comprise destilling tower, flash column, compressor, liquid outlet bottom described destilling tower connects the inlet of flash column, the exhaust outlet at flash column top connects the air inlet of compressor, the exhaust outlet of compressor connects the air inlet of destilling tower bottom, the exhaust outlet at described destilling tower top is provided with connecting pipe, connecting pipe is provided with heat exchanger, the inlet of this heat exchanger is connected with the liquid outlet of flash column, the liquid outlet of heat exchanger is connected with the inlet on flash column top, the feed pipe of described destilling tower is also provided with heat exchanger, the inlet of this heat exchanger connects the liquid outlet of flash column, the liquid outlet of heat exchanger connects another heat exchanger.
The present invention is according to heat pump technical principle, by connecting flash column at the bottom of destilling tower, the flash distillation of still liquid is formed flash-off steam, and flash column is connected with the reflux line of destilling tower by heat exchanger, sends to flash distillation again after the steam achieving the still liquid after flash distillation and tower top carries out heat exchange; Simultaneously, reclaim the flash steam after the heat of still liquid at the bottom of overhead vapours and tower, after being done work by compressor compresses, make it to become high-temperature high-pressure overheat steam, and sent into bottom destilling tower, in order to heating and vaporization still liquid, thus achieve recycling while still liquid low temperature exhaust heat at the bottom of overhead vapours and tower.
The present invention can on the basis keeping former destilling tower operating condition completely, completely without the need to consuming heating steam within other system cloud gray model phase except the system starting period.Therefore, the present invention, compared with Conventional espresso method, has the advantage that significantly can improve energy utilization rate, significantly reduce distillation energy consumption.Such as, SO is absorbed at doctor solution 2from solution, SO in solution is reclaimed afterwards by distillation 2process in, in ammonia distillation process, at employing MEDA de-H from gas 2s, CO 2from solution, H in solution is reclaimed afterwards by distillation 2s, CO 2process in, when adopting heat pump distillation flow process of the present invention to distill, it can save energy more than 75% compared with employing Conventional espresso method.
Described connecting pipe is provided with the heat exchanger be connected with feed pipe.
In described connecting pipe, count from the air inlet of connecting pipe, be followed successively by the heat exchanger be connected with flash column, the heat exchanger be connected with feed pipe.Achieve steam first with flash liquid heat exchange, then with feed liquid heat exchange, the advantage of this order is that heat exchange area reduces, and at utmost reclaims heat.
Preferably, in described connecting pipe, after the heat exchanger be connected with feed pipe, be also provided with a heat exchanger.
Preferably, in described connecting pipe, after the heat exchanger be connected with feed pipe, be also disposed with a heat exchanger and a gas-liquid separator.Steam after heat exchange is after water-cooled, gas-liquid separation, and gas recovery, liquid backflow is to destilling tower.
The liquid outlet of described gas-liquid separator connects destilling tower.
The air inlet distance bottom 2-6m of described destilling tower bottom.
The compression ratio of described compressor is 1.8-4.
Low energy consumption and efficient heat utilization efficiency is possessed for realizing still-process, therefore with compressor to flash-off steam compressed action time, the compression ratio of compressor need be considered, compression ratio is set as 1.8-4 by the present invention, this is mainly because too high compression ratio can cause compressor shaft power too high, energy-saving efficiency declines, and the too low then energy-saving effect of compression ratio is not remarkable.
The absolute pressure of described compressor outlet steam is 0.12 ~ 0.3MPa, and temperature is 104-133 DEG C.
From taking into account suitable compressor shaft power and suitable compressor outlet superheat steam temperature, the gauge pressure of setting flash steam compressor outlet superheated steam after compressor compression is 0.12-0.3MPa, temperature is 104-160 DEG C, do not need by tower bottom reboiler and lean solution heat exchange, only need slightly high compared with the temperature and pressure bottom destilling tower, the shaft power of compressor is low, and energy consumption is low.
The temperature of described flash distillation is 75 DEG C ~ 120 DEG C, and pressure is 0.04MPa ~ 0.2 MPa.
Beneficial effect of the present invention is:
1, heat pump distillation energy saver of the present invention on the basis keeping former destilling tower operating condition completely, can need except the system starting period to consume more steam, is only needing to consume a small amount of heating steam during normal operation.Therefore, the present invention, compared with Conventional espresso method, has the advantage that significantly can improve energy utilization rate, significantly reduce distillation energy consumption.Such as, SO is absorbed at doctor solution 2from solution, SO in solution is reclaimed afterwards by distillation 2process in, in ammonia distillation process, at employing MEDA de-H from gas 2s, CO 2from solution, H in solution is reclaimed afterwards by distillation 2s, CO 2process in, when adopting heat pump distillation flow process of the present invention to distill, it can save energy more than 75% compared with employing Conventional espresso method.
2, the flash steam compressed action that produces after heat being reclaimed to still liquid at the bottom of destilling tower and overhead vapours by compressor of the present invention, become high-temperature high-pressure overheat steam, and with this superheated steam for thermal source heats distillation tower reactor still liquid and vaporizes, thus the recycling achieved still liquid low temperature exhaust heat at the bottom of overhead vapours and tower, and form the heat pump distillation flow process with high energy efficiency, low energy consumption, low operating cost feature with this.Can be widely used in the Distallation systm in the industries such as petrochemical industry, metallurgy, chemical industry, environmental protection, have broad application prospects.
3, the high-temperature high-pressure overheat steam that compressor exports by the present invention directly enters in destilling tower at the bottom of tower, by the heat of still liquid and overhead vapours at the bottom of recovery tower, cooling water inflow needed for overhead vapours compares can significantly be reduced with common distil process, thus is conducive to the operating cost reducing distillation further.
4, flash evaporation technology and heat pump techniques organically combine by the present invention, for the proposition one of energy-saving distillation consumption reduction has the technology of novelty, efficiently solve the problem that Conventional espresso process steam consumption is high, running cost is high; Steam after compression is directly entered at the bottom of destilling tower tower, is not needed the still liquid heat exchange at the bottom of reboiler and tower, the vapor (steam) temperature after compression and pressure lower, heat transfer efficiency is high, and technological process is simply, easy to operate, small investment.
5, the present invention utilizes flash evaporation technology not only to make the heat in still liquid be recycled, and after flash distillation, reduce further the volatile components content in still liquid, by other supporting techniques of distillation provide strong guarantee.
Accompanying drawing explanation
Fig. 1 is the structural representation of the heat pump distillation energy saver of the embodiment of the present invention 1.
Fig. 2 is the structural representation of the heat pump distillation energy saver of the embodiment of the present invention 5.
Fig. 3 is the structural representation of the heat pump distillation energy saver of the embodiment of the present invention 7.
Be labeled as in figure: 1, destilling tower, 2, heat exchanger, 3, heat exchanger, 4, heat exchanger, 5, gas-liquid separator, 6, flash distillation liquid pump, 7, flash column, 8, compressor, 9, heat exchanger, 10, heat exchanger, 11, reflux pump, 12, reboiler, 13, connecting pipe, 14, feed pipe, 15, heat exchanger exhaust outlet.
Detailed description of the invention
Below in conjunction with detailed description of the invention, essentiality content of the present invention is described in further detail.
Embodiment 1
A kind of heat pump distillation energy saver, comprise destilling tower 1, flash column 7, compressor 8, liquid outlet bottom described destilling tower 1 connects the inlet of flash column 7, the exhaust outlet at flash column 7 top connects the air inlet of compressor 8, the exhaust outlet of compressor 8 connects the air inlet of destilling tower 1 bottom, the exhaust outlet at described destilling tower 1 top is provided with connecting pipe 13, connecting pipe 13 is provided with heat exchanger 2, the inlet of this heat exchanger 2 is connected with the liquid outlet of flash column 7, the liquid outlet of heat exchanger 2 is connected with the inlet on flash column 7 top, the feed pipe 14 of described destilling tower 1 is also provided with heat exchanger 9, the inlet of this heat exchanger 9 connects the liquid outlet of flash column 7, the liquid outlet of heat exchanger 9 connects another heat exchanger 10.
Embodiment 2
A kind of heat pump distillation energy saver, comprise destilling tower 1, flash column 7, compressor 8, liquid outlet bottom described destilling tower 1 connects the inlet of flash column 7, the exhaust outlet at flash column 7 top connects the air inlet of compressor 8, the exhaust outlet of compressor 8 connects the air inlet of destilling tower 1 bottom, the exhaust outlet at described destilling tower 1 top is provided with connecting pipe 13, connecting pipe 13 is provided with heat exchanger 2, the inlet of this heat exchanger 2 is connected with the liquid outlet of flash column 7, the liquid outlet of heat exchanger 2 is connected with the inlet on flash column 7 top, the feed pipe 14 of described destilling tower 1 is also provided with heat exchanger 9, the inlet of this heat exchanger 9 connects the liquid outlet of flash column 7, the liquid outlet of heat exchanger 9 connects another heat exchanger 10.
The exhaust outlet 15 of described heat exchanger 2 is connected to lower operation.
Embodiment 3
A kind of heat pump distillation energy saver, comprise destilling tower 1, flash column 7, compressor 8, liquid outlet bottom described destilling tower 1 connects the inlet of flash column 7, the exhaust outlet at flash column 7 top connects the air inlet of compressor 8, the exhaust outlet of compressor 8 connects the air inlet of destilling tower 1 bottom, the exhaust outlet at described destilling tower 1 top is provided with connecting pipe 13, connecting pipe 13 is provided with heat exchanger 2, the inlet of this heat exchanger 2 is connected with the liquid outlet of flash column 7, the liquid outlet of heat exchanger 2 is connected with the inlet on flash column 7 top, the feed pipe 14 of described destilling tower 1 is also provided with heat exchanger 9, the inlet of this heat exchanger 9 connects the liquid outlet of flash column 7, the liquid outlet of heat exchanger 9 connects another heat exchanger 10.
Described connecting pipe 13 is provided with the heat exchanger 3 be connected with feed pipe 14.
Embodiment 4
A kind of heat pump distillation energy saver, comprise destilling tower 1, flash column 7, compressor 8, liquid outlet bottom described destilling tower 1 connects the inlet of flash column 7, the exhaust outlet at flash column 7 top connects the air inlet of compressor 8, the exhaust outlet of compressor 8 connects the air inlet of destilling tower 1 bottom, the exhaust outlet at described destilling tower 1 top is provided with connecting pipe 13, connecting pipe 13 is provided with heat exchanger 2, the inlet of this heat exchanger 2 is connected with the liquid outlet of flash column 7, the liquid outlet of heat exchanger 2 is connected with the inlet on flash column 7 top, the feed pipe 14 of described destilling tower 1 is also provided with heat exchanger 9, the inlet of this heat exchanger 9 connects the liquid outlet of flash column 7, the liquid outlet of heat exchanger 9 connects another heat exchanger 10.
Described connecting pipe 13 is provided with the heat exchanger 3 be connected with feed pipe 14.
In described connecting pipe 13, count from the air inlet of connecting pipe 13, be followed successively by the heat exchanger 2 be connected with flash column 7, the heat exchanger 3 be connected with feed pipe 14.
Embodiment 5
A kind of heat pump distillation energy saver, comprise destilling tower 1, flash column 7, compressor 8, liquid outlet bottom described destilling tower 1 connects the inlet of flash column 7, the exhaust outlet at flash column 7 top connects the air inlet of compressor 8, the exhaust outlet of compressor 8 connects the air inlet of destilling tower 1 bottom, the exhaust outlet at described destilling tower 1 top is provided with connecting pipe 13, connecting pipe 13 is provided with heat exchanger 2, the inlet of this heat exchanger 2 is connected with the liquid outlet of flash column 7, the liquid outlet of heat exchanger 2 is connected with the inlet on flash column 7 top, the feed pipe 14 of described destilling tower 1 is also provided with heat exchanger 9, the inlet of this heat exchanger 9 connects the liquid outlet of flash column 7, the liquid outlet of heat exchanger 9 connects another heat exchanger 10.
Described connecting pipe 13 is provided with the heat exchanger 3 be connected with feed pipe 14.
In described connecting pipe 13, count from the air inlet of connecting pipe 13, be followed successively by the heat exchanger 2 be connected with flash column 7, the heat exchanger 3 be connected with feed pipe 14.
In described connecting pipe 13, the heat exchanger 3 be connected with feed pipe 14 is also provided with a heat exchanger 4 below.
Embodiment 6
A kind of heat pump distillation energy saver, comprise destilling tower 1, flash column 7, compressor 8, liquid outlet bottom described destilling tower 1 connects the inlet of flash column 7, the exhaust outlet at flash column 7 top connects the air inlet of compressor 8, the exhaust outlet of compressor 8 connects the air inlet of destilling tower 1 bottom, the exhaust outlet at described destilling tower 1 top is provided with connecting pipe 13, connecting pipe 13 is provided with heat exchanger 2, the inlet of this heat exchanger 2 is connected with the liquid outlet of flash column 7, the liquid outlet of heat exchanger 2 is connected with the inlet on flash column 7 top, the feed pipe 14 of described destilling tower 1 is also provided with heat exchanger 9, the inlet of this heat exchanger 9 connects the liquid outlet of flash column 7, the liquid outlet of heat exchanger 9 connects another heat exchanger 10.
Described connecting pipe 13 is provided with the heat exchanger 3 be connected with feed pipe 14.
In described connecting pipe 13, count from the air inlet of connecting pipe 13, be followed successively by the heat exchanger 2 be connected with flash column 7, the heat exchanger 3 be connected with feed pipe 14.
In described connecting pipe 13, the heat exchanger 3 be connected with feed pipe 14 is also disposed with a heat exchanger 4 and a gas-liquid separator 5 below.
Embodiment 7
A kind of heat pump distillation energy saver, comprise destilling tower 1, flash column 7, compressor 8, liquid outlet bottom described destilling tower 1 connects the inlet of flash column 7, the exhaust outlet at flash column 7 top connects the air inlet of compressor 8, the exhaust outlet of compressor 8 connects the air inlet of destilling tower 1 bottom, the exhaust outlet at described destilling tower 1 top is provided with connecting pipe 13, connecting pipe 13 is provided with heat exchanger 2, the inlet of this heat exchanger 2 is connected with the liquid outlet of flash column 7, the liquid outlet of heat exchanger 2 is connected with the inlet on flash column 7 top, the feed pipe 14 of described destilling tower 1 is also provided with heat exchanger 9, the inlet of this heat exchanger 9 connects the liquid outlet of flash column 7, the liquid outlet of heat exchanger 9 connects another heat exchanger 10.
Described connecting pipe 13 is provided with the heat exchanger 3 be connected with feed pipe 14.
In described connecting pipe 13, count from the air inlet of connecting pipe 13, be followed successively by the heat exchanger 2 be connected with flash column 7, the heat exchanger 3 be connected with feed pipe 14.
In described connecting pipe 13, the heat exchanger 3 be connected with feed pipe 14 is also disposed with a heat exchanger 4 and a gas-liquid separator 5 below.
The liquid outlet of described gas-liquid separator 5 connects destilling tower 1.
Embodiment 8
A kind of heat pump distillation energy saver, comprise destilling tower 1, flash column 7, compressor 8, liquid outlet bottom described destilling tower 1 connects the inlet of flash column 7, the exhaust outlet at flash column 7 top connects the air inlet of compressor 8, the exhaust outlet of compressor 8 connects the air inlet of destilling tower 1 bottom, the exhaust outlet at described destilling tower 1 top is provided with connecting pipe 13, connecting pipe 13 is provided with heat exchanger 2, the inlet of this heat exchanger 2 is connected with the liquid outlet of flash column 7, the liquid outlet of heat exchanger 2 is connected with the inlet on flash column 7 top, the feed pipe 14 of described destilling tower 1 is also provided with heat exchanger 9, the inlet of this heat exchanger 9 connects the liquid outlet of flash column 7, the liquid outlet of heat exchanger 9 connects another heat exchanger 10.
Described connecting pipe 13 is provided with the heat exchanger 3 be connected with feed pipe 14.
In described connecting pipe 13, count from the air inlet of connecting pipe 13, be followed successively by the heat exchanger 2 be connected with flash column 7, the heat exchanger 3 be connected with feed pipe 14.
In described connecting pipe 13, the heat exchanger 3 be connected with feed pipe 14 is also disposed with a heat exchanger 4 and a gas-liquid separator 5 below.
The liquid outlet of described gas-liquid separator 5 connects destilling tower 1.
The air inlet distance bottom 6m of described destilling tower 1 bottom.
Embodiment 9
A kind of heat pump distillation energy saver, comprise destilling tower 1, flash column 7, compressor 8, liquid outlet bottom described destilling tower 1 connects the inlet of flash column 7, the exhaust outlet at flash column 7 top connects the air inlet of compressor 8, the exhaust outlet of compressor 8 connects the air inlet of destilling tower 1 bottom, the exhaust outlet at described destilling tower 1 top is provided with connecting pipe 13, connecting pipe 13 is provided with heat exchanger 2, the inlet of this heat exchanger 2 is connected with the liquid outlet of flash column 7, the liquid outlet of heat exchanger 2 is connected with the inlet on flash column 7 top, the feed pipe 14 of described destilling tower 1 is also provided with heat exchanger 9, the inlet of this heat exchanger 9 connects the liquid outlet of flash column 7, the liquid outlet of heat exchanger 9 connects another heat exchanger 10.
Described connecting pipe 13 is provided with the heat exchanger 3 be connected with feed pipe 14.
In described connecting pipe 13, count from the air inlet of connecting pipe 13, be followed successively by the heat exchanger 2 be connected with flash column 7, the heat exchanger 3 be connected with feed pipe 14.
In described connecting pipe 13, the heat exchanger 3 be connected with feed pipe 14 is also provided with a heat exchanger 4 below.
The air inlet distance bottom 2m of described destilling tower 1 bottom.
The absolute pressure of described compressor 8 outlet vapor is 0.18MPa, and temperature is 115 DEG C.
Embodiment 10
A kind of heat pump distillation energy saver, comprise destilling tower 1, flash column 7, compressor 8, liquid outlet bottom described destilling tower 1 connects the inlet of flash column 7, the exhaust outlet at flash column 7 top connects the air inlet of compressor 8, the exhaust outlet of compressor 8 connects the air inlet of destilling tower 1 bottom, the exhaust outlet at described destilling tower 1 top is provided with connecting pipe 13, connecting pipe 13 is provided with heat exchanger 2, the inlet of this heat exchanger 2 is connected with the liquid outlet of flash column 7, the liquid outlet of heat exchanger 2 is connected with the inlet on flash column 7 top, the feed pipe 14 of described destilling tower 1 is also provided with heat exchanger 9, the inlet of this heat exchanger 9 connects the liquid outlet of flash column 7, the liquid outlet of heat exchanger 9 connects another heat exchanger 10.
Described connecting pipe 13 is provided with the heat exchanger 3 be connected with feed pipe 14.
The air inlet distance bottom 3m of described destilling tower 1 bottom.
The absolute pressure of described compressor 8 outlet vapor is 0.12MPa, and temperature is 104 DEG C.
The temperature of described flash distillation is 75 DEG C, and pressure is 0.04MPa.
Embodiment 11
A kind of heat pump distillation energy saver, comprise destilling tower 1, flash column 7, compressor 8, liquid outlet bottom described destilling tower 1 connects the inlet of flash column 7, the exhaust outlet at flash column 7 top connects the air inlet of compressor 8, the exhaust outlet of compressor 8 connects the air inlet of destilling tower 1 bottom, the exhaust outlet at described destilling tower 1 top is provided with connecting pipe 13, connecting pipe 13 is provided with heat exchanger 2, the inlet of this heat exchanger 2 is connected with the liquid outlet of flash column 7, the liquid outlet of heat exchanger 2 is connected with the inlet on flash column 7 top, the feed pipe 14 of described destilling tower 1 is also provided with heat exchanger 9, the inlet of this heat exchanger 9 connects the liquid outlet of flash column 7, the liquid outlet of heat exchanger 9 connects another heat exchanger 10.
Described connecting pipe 13 is provided with the heat exchanger 3 be connected with feed pipe 14.
In described connecting pipe 13, count from the air inlet of connecting pipe 13, be followed successively by the heat exchanger 2 be connected with flash column 7, the heat exchanger 3 be connected with feed pipe 14.
In described connecting pipe 13, the heat exchanger 3 be connected with feed pipe 14 is also disposed with a heat exchanger 4 and a gas-liquid separator 5 below.
The liquid outlet of described gas-liquid separator 5 connects destilling tower 1.
The air inlet distance bottom 4m of described destilling tower 1 bottom.
The compression ratio of described compressor is 4.
The absolute pressure of described compressor 8 outlet vapor is 0.3MPa, and temperature is 133 DEG C.
The temperature of described flash distillation is 120 DEG C, and pressure is 0.2 MPa.
Embodiment 12
A kind of heat pump distillation energy saver, comprise destilling tower 1, flash column 7, compressor 8, liquid outlet bottom described destilling tower 1 connects the inlet of flash column 7, the exhaust outlet at flash column 7 top connects the air inlet of compressor 8, the exhaust outlet of compressor 8 connects the air inlet of destilling tower 1 bottom, the exhaust outlet at described destilling tower 1 top is provided with connecting pipe 13, connecting pipe 13 is provided with heat exchanger 2, the inlet of this heat exchanger 2 is connected with the liquid outlet of flash column 7, the liquid outlet of heat exchanger 2 is connected with the inlet on flash column 7 top, the feed pipe 14 of described destilling tower 1 is also provided with heat exchanger 9, the inlet of this heat exchanger 9 connects the liquid outlet of flash column 7, the liquid outlet of heat exchanger 9 connects another heat exchanger 10.
Described connecting pipe 13 is provided with the heat exchanger 3 be connected with feed pipe 14.
In described connecting pipe 13, count from the air inlet of connecting pipe 13, be followed successively by the heat exchanger 2 be connected with flash column 7, the heat exchanger 3 be connected with feed pipe 14.
In described connecting pipe 13, the heat exchanger 3 be connected with feed pipe 14 is also disposed with a heat exchanger 4 and a gas-liquid separator 5 below.
The liquid outlet of described gas-liquid separator 5 connects destilling tower 1.
The air inlet distance bottom 3m of described destilling tower 1 bottom.
The compression ratio of described compressor is 1.8.
The absolute pressure of described compressor 8 outlet vapor is 0.2MPa, and temperature is 120 DEG C.
The temperature of described flash distillation is 105 DEG C, and pressure is 0.1MPa.
Embodiment 13
A kind of heat pump distillation energy saver, comprise destilling tower 1, flash column 7, compressor 8, liquid outlet bottom described destilling tower 1 connects the inlet of flash column 7, the exhaust outlet at flash column 7 top connects the air inlet of compressor 8, the exhaust outlet of compressor 8 connects the air inlet of destilling tower 1 bottom, the exhaust outlet at described destilling tower 1 top is provided with connecting pipe 13, connecting pipe 13 is provided with heat exchanger 2, the inlet of this heat exchanger 2 is connected with the liquid outlet of flash column 7, the liquid outlet of heat exchanger 2 is connected with the inlet on flash column 7 top, the feed pipe 14 of described destilling tower 1 is also provided with heat exchanger 9, the inlet of this heat exchanger 9 connects the liquid outlet of flash column 7, the liquid outlet of heat exchanger 9 connects another heat exchanger 10.
Described connecting pipe 13 is provided with the heat exchanger 3 be connected with feed pipe 14.
In described connecting pipe 13, count from the air inlet of connecting pipe 13, be followed successively by the heat exchanger 2 be connected with flash column 7, the heat exchanger 3 be connected with feed pipe 14.
In described connecting pipe 13, the heat exchanger 3 be connected with feed pipe 14 is also disposed with a heat exchanger 4 and a gas-liquid separator 5 below.
The liquid outlet of described gas-liquid separator 5 connects destilling tower 1.
The air inlet distance bottom 3m of described destilling tower 1 bottom.
The compression ratio of described compressor is 3.
The absolute pressure of described compressor 8 outlet vapor is 0.25MPa, and temperature is 125 DEG C.
The temperature of described flash distillation is 110 DEG C, and pressure is 0.12MPa.
Embodiment 14
The heat pump distillation (device is if Fig. 3 is as shown) of desulfurization solvent when heat pump distillation energy saver of the present invention is used for the solvent cycle absorption method flue gas desulfurization of steel works sintering flue gas:
From desulfurizing tower containing SO 2desulfurization solvent rich solution through poor rich liquid heat exchanger with from flash column lean solution heat exchange and be heated to 90 DEG C;
0.19MPa(absolute pressure from distillation tower top produces), after the steam of the 118 DEG C lean solution heat exchange with flash column, then with rich or poor liquid heat exchange after rich solution heat exchange, steam by water cooling to 45 DEG C; The lean solution that flash column comes is warmed up to 116 DEG C, turns back to flash column, and destilling tower sent into by rich solution.
Rich solution carries out counter current contacting with upflowing vapor in tower reactor on inner-tower filling material, by heating, stripping effect, distills out wherein contained SO 2.After distillation, gained desulfurization solvent lean solution delivers to flash column from destilling tower, and form flash steam by flash distillation, flash steam delivers to destilling tower inner bottom part after compressor compresses, and the steam formed with the water of components vaporize forms the upflowing vapor in tower in the lump.
Lean solution after flash distillation, after poor rich liquid heat exchanger and rich solution heat exchange, enters lean solution cooler, send desulfurization section to recycle after water-cooled cooling to 45 DEG C.
In flash column, absolute pressure is 0.07MPa, and flash steam temperature is 89 DEG C, and flash steam enters compressor, and by compressor to its compressed action, becoming pressure is 0.25MPa(absolute pressure), temperature is the superheated steam of 160 DEG C.The superheated steam that compressor exports delivers to bottom in destilling tower, in destilling tower by lean solution heating temperatures to 123 DEG C, form the upflowing vapor in destilling tower together with the part water of vaporization.
Embodiment 15
Heat pump distillation energy saver of the present invention is used for residual coking ammonia water heat pump distillation (device is if Fig. 1 is as shown):
The present embodiment chooses coking ammonia water, and treating capacity is 60t/h, containing ammonia density 6000 mg/L.Enter ammonia distillation tower after the distilled ammonia wastewater heat exchange of the ammoniacal liquor sent here from battery limit (BL) and flash column, ammonia distillation tower top pressure is 0.12MPa(absolute pressure), tower top temperature is 105 DEG C, and tower bottom pressure is 0.14MPa(absolute pressure), column bottom temperature is 109 DEG C.
Distilled ammonia wastewater at the bottom of ammonia distillation tower delivers to flash column, distilled ammonia wastewater after flash distillation returns flash column after delivering to ammonia distillation tower top and tower top ammonia steam heat-exchanging, with 10 times that the distilled ammonia wastewater amount after the vapor heated flash distillation of ammonia is the ammonia vol entering ammonia still, the temperature after ammonia steam heat-exchanging is 95 DEG C ~ 102 DEG C and delivers to lower operation.
Distilled ammonia wastewater is flash distillation in flash column, and flashing pressure is 0.05 MPa, and temperature is 81 DEG C, and flash steam is forced into 0.18MPa by vapour compression machine, temperature delivers to ammonia still inner bottom part after being increased to 148 ° of C, as the thermal source of ammonia distillation.Meanwhile, the effluent part in flash column, through with remained ammonia heat exchange, water cooling after enter lower operation.Ammonia distillation tower goes into operation to be needed to adopt steam, can directly directly pass in ammonia distillation tower by the live steam outside battery limit (BL), also can arrange in a reboiler and pass into live steam indirect distilled ammonia wastewater.
Adopt as above technology, its processed waste water reduces, and process ton remained ammonia was reduced to below 50Kg by originally needing the steam 175Kg of 0.6MPa.
Embodiment 16
Heat pump distillation energy saver of the present invention is used for Gas Purification Factory MEDA desulfuration solution and takes off H 2s:
Gas Purification Factory adopts the amine desulphurization solvents such as MEDA to remove H from natural gas 2s, CO 2, absorb H 2s, CO 2deng the rich solution of sour gas, rich solution after flash distillation, by being pumped into the lean solution heat exchange to 65 after heat exchanger and flash distillation DEG C ~ 90 DEG C, rich solution again with the lean solution heat exchange after flash distillation after overhead vapours heat exchange after 100 DEG C ~ 110 DEG C, enter destilling tower, lean solution at the bottom of destilling tower delivers to flash column, flash steam after flash distillation, by directly sending into destilling tower inner bottom part after compressor compresses, returns flash column after the lean solution part after flash distillation delivers to the steam heat-exchanging of tower top and destilling tower again; After water cooling is to 40 DEG C ~ 50 DEG C, absorption tower is delivered to again after part lean solution delivers to heat exchanger and rich solution heat exchange.After the lean solution heat exchange after flash distillation of the steam of tower top again with rich solution heat exchange, finally by water cooling to 30 DEG C ~ 50 DEG C, obtain concentration higher containing H 2s, CO 2deng sour gas, deliver to lower operation.
Lean solution flashing pressure controls 0.05 MPa ~ 0.11 MPa, temperature is 81 DEG C ~ 101 DEG C, flash steam is forced into 0.14MPa ~ 0.24MPa by vapour compression machine, temperature delivers to destilling tower inner bottom part after being increased to 120 ° of C ~ 180 ° C, as the thermal source of the amine desulphurization solvent distillations such as MEDA.
Embodiment 17
Heat pump distillation energy saver of the present invention is used for coke oven gas desulfurization, adopts SUIFIBAN method to remove coke-stove gas H 2s, HCN and CO 2, the de-heat pump distillation that adopts of desulfuration solution is separated H 2s, HCN and CO 2:
SUIFIBAN technique by desulfuration and decyanation with 15% MEA as desulfurizing agent, absorb the H in coke-stove gas under cryogenic 2s, HCN and CO 2, then the sour gas in solution is parsed with steam distillation.
Absorb H 2s, HCN, CO 2deng the rich solution of sour gas, by being pumped into the lean solution heat exchange to 65 after heat exchanger and flash distillation DEG C ~ 90 DEG C, rich solution again with the lean solution heat exchange after flash distillation after overhead vapours heat exchange after 100 DEG C ~ 110 DEG C, enter destilling tower, lean solution at the bottom of destilling tower delivers to flash column, flash steam after flash distillation, by directly sending into destilling tower inner bottom part after compressor compresses, returns flash column after the lean solution part after flash distillation delivers to the steam heat-exchanging of tower top and destilling tower again; After water cooling is to 25 DEG C ~ 28 DEG C, absorption tower is delivered to again after part lean solution delivers to heat exchanger and rich solution heat exchange.After the lean solution heat exchange after flash distillation of the steam of tower top again with rich solution heat exchange, finally by water cooling to 30 DEG C ~ 50 DEG C, obtain concentration higher containing H 2s, CO 2deng sour gas, deliver to lower operation.
Lean solution flashing pressure controls 0.075 MPa ~ 0.09 MPa, temperature is 91 DEG C ~ 98 DEG C, flash steam is forced into 0.14MPa ~ 0.18MPa by vapour compression machine, temperature delivers to destilling tower inner bottom part after being increased to 120 ° of C ~ 156 ° C, as the thermal source of the amine desulphurization solvent distillations such as MEDA.
Embodiment 18
With heat pump distillation energy saver of the present invention for distillation equipment, for the aqueous solution of hot wet chemical, ethanolamines as absorbent or using other aqueous solution as absorbent, from gas, absorb CO 2after adopt heat pump distillation mode to obtain high-purity CO again 2:
Using the aqueous solution of hot wet chemical, ethanolamines as absorbent or using other aqueous solution as absorbent, from gas, absorb CO 2after rich solution, by being pumped into the lean solution heat exchange to 75 after heat exchanger and flash distillation DEG C ~ 90 DEG C, rich solution again with the lean solution heat exchange after flash distillation after overhead vapours heat exchange after 102 DEG C ~ 106 DEG C, enter destilling tower, lean solution at the bottom of destilling tower delivers to flash column, flash steam after flash distillation, by directly sending into destilling tower inner bottom part after compressor compresses, returns flash column after the lean solution part after flash distillation delivers to the steam heat-exchanging of tower top and destilling tower again; After water cooling is to 30 DEG C ~ 50 DEG C, absorption tower is delivered to again after part lean solution delivers to heat exchanger and rich solution heat exchange.After the lean solution heat exchange after flash distillation of the steam of tower top again with rich solution heat exchange, finally by water cooling to 30 DEG C ~ 50 DEG C, high concentration CO 2gas, delivers to lower operation.
Lean solution flashing pressure controls 0.065 MPa ~ 0.11 MPa, and temperature is 88 DEG C ~ 102 DEG C, and flash steam is forced into 0.15MPa ~ 0.22MPa by vapour compression machine, temperature delivers to destilling tower inner bottom part after being increased to 115 ° of C ~ 190 ° C, as the thermal source of decarbonizing solution distillation.
As can be seen here, a kind of heat pump distillation energy saver of the present invention, compared with conventional non-heat pump distilling apparatus, possesses the advantage of obvious low energy consumption, high energy efficiency, low operating cost.Have heat recovery efficiency high compared with other heat pump distillation devices, the high-temperature steam of compression does not need by reboiler indirect, the vapor (steam) temperature after compression and pressure lower, the advantage that the power consumption of compressor is low.

Claims (9)

1. a heat pump distillation energy saver, it is characterized in that: comprise destilling tower (1), flash column (7), compressor (8), the liquid outlet of described destilling tower (1) bottom connects the inlet of flash column (7), the exhaust outlet at flash column (7) top connects the air inlet of compressor (8), the exhaust outlet of compressor (8) connects the air inlet of destilling tower (1) bottom, the exhaust outlet at described destilling tower (1) top is provided with connecting pipe (13), connecting pipe (13) is provided with heat exchanger (2), the inlet of this heat exchanger (2) is connected with the liquid outlet of flash column (7), the liquid outlet of heat exchanger (2) is connected with the inlet on flash column (7) top, the feed pipe (14) of described destilling tower (1) is also provided with heat exchanger (9), the inlet of this heat exchanger (9) connects the liquid outlet of flash column (7), the liquid outlet of heat exchanger (9) connects another heat exchanger (10).
2. a kind of heat pump distillation energy saver according to claim 1, is characterized in that: described connecting pipe (13) is provided with the heat exchanger (3) be connected with feed pipe (14).
3. a kind of heat pump distillation energy saver according to claim 2, it is characterized in that: in described connecting pipe (13), count from the air inlet of connecting pipe (13), be followed successively by the heat exchanger (2) be connected with flash column (7), the heat exchanger (3) be connected with feed pipe (14).
4. a kind of heat pump distillation energy saver according to claim 3, is characterized in that: in described connecting pipe (13), and the heat exchanger (3) be connected with feed pipe (14) is also provided with a heat exchanger (4) below.
5. a kind of heat pump distillation energy saver according to claim 3, it is characterized in that: in described connecting pipe (13), the heat exchanger (3) be connected with feed pipe (14) is also disposed with a heat exchanger (4) and a gas-liquid separator (5) below.
6. a kind of heat pump distillation energy saver according to claim 5, is characterized in that: the liquid outlet of described gas-liquid separator (5) connects destilling tower (1).
7. a kind of heat pump distillation energy saver according to claim 1, is characterized in that: the air inlet distance bottom 2-6m of described destilling tower (1) bottom.
8. a kind of heat pump distillation energy saver according to claim 1, is characterized in that: the compression ratio of described compressor (8) is 1.8-4.
9. a kind of heat pump distillation energy saver according to claim 1, is characterized in that: the absolute pressure of described compressor (8) outlet vapor is 0.12 ~ 0.3MPa, and temperature is 104 ~ 133 DEG C.
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