CN104056461A - Novel energy-saving distillation technology of heat pump - Google Patents
Novel energy-saving distillation technology of heat pump Download PDFInfo
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- CN104056461A CN104056461A CN201410328909.XA CN201410328909A CN104056461A CN 104056461 A CN104056461 A CN 104056461A CN 201410328909 A CN201410328909 A CN 201410328909A CN 104056461 A CN104056461 A CN 104056461A
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Abstract
The invention provides a novel energy-saving distillation technology of a heat pump, aiming at reducing the device energy consumption of distillation of the heat pump and simplifying the process. The technology comprises the following steps: A. conveying a kettle solution at the bottom of a distillation column to a flash column, and performing flashing in the flash column; B. introducing flashing steam generated by flashing into a compressor, and carrying out compression on the flashing steam for acting by the compressor; C. introducing steam output by the compressor to the bottom in the distillation column, forming rising steam required for distillation by the steam output by the compressor and a vaporized kettle solution, and transferring mass and heat between the rising steam and a liquid declining from the upper part of the distillation column in a backflow mode to complete the distillation process; exchanging heat between partial kettle solution subjected to flashing with steam discharged from the top of the distillation column, and returning to the flash column after recycling heat of the steam; and exchanging heat of the residual kettle solution subjected to flashing with a material liquid entering the distillation column, and carrying out water cooling and recycling after recycling the heat of the kettle solution. The novel distillation technology provided by the invention is simple in technological process, low in investment and high in energy saving efficiency, and can save more than 70% of energy compared with a traditional distillation method.
Description
Technical field
The present invention relates to heat pump distillation technical field, be specifically related to a kind of heat pump distillation new energy-saving process.
Background technology
Chemical industry is energy consumption rich and influential family, and wherein distillation is again the high unit operations of energy consumption, and traditional distillation mode thermodynamic efficiency is very low, and energy dissipation is very large.As document " application of the rich renewable amine method desulfur technology of health generation " (< < sulfuric acid industry > >, 2007 (1): pass through separated SO 39-45) from desulfurization absorption liquid
2, sweetening liq per ton need consume the saturated vapor of 0.1-0.2t0.6MPa; " 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), from coking ammonia water, pass through the ammonia in separated solution, 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
2by distillation, from solution, reclaim H in solution afterwards
2s, CO
2, the document analyzed MDEA method desulfurization energy flow situation, and surplus solution per ton also needs to consume the saturated vapor of 150-200Kg0.6MPa, has proposed to adopt after the sour gas of heat pump compression distillation tower top for the lean solution at the bottom of reboiler heating tower.
In the situation that 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.These people have been proposed to many conservation measures, by a large amount of theory analysises, experimental study and commercial Application, shown, wherein energy-saving effect is heat pump distillation technology very significantly.Heat pump techniques is that the energy recovery receiving much attention in the world is in recent years utilized technology, and it mainly, by consuming a part of mechanical energy, electric energy etc. for compensation, makes heat energy realize the transmission from low-temperature heat source to high temperature heat source.Because heat pump can be converted to high temperature heat by low temperature heat energy, improve the effective rate of utilization of the energy, be therefore the important channel of reclaiming low temperature exhaust heat.
The general heat pump distillation that adopts heats up the pressurization of destilling tower overhead vapours, makes its thermal source that is used as tower bottom reboiler, reclaims the condensation latent heat of overhead vapours.In document " the heat-pump rectifying process process analysis in energy saving of chemical industry " (the energy-conservation > > of < <, 2004 (10): described multiple heat pump distillation flow process 19-22).But it is significantly not enough that these flow processs exist when concrete application, and major defect is:
1, invest high, technological process is complicated, high concentration poisonous and harmful medium directly adopts compressor compresses, compressor seriously corroded or material rate require high, heat recovery is insufficient;
2, the gas after compression, containing incoagulable gas, causes reboiler heat transfer efficiency low, and reboiler operating pressure is high, perishable;
As coking ammonia water, distillation is used any flow process in above-mentioned document all to have the problems such as seriously corroded or material rate require height, obstruction, flow process is complicated, recuperation of heat is insufficient.
201110128227.0, name is called the patent of invention of " heat pump of desulfurization solvent regeneration flow process in solvent cycle absorption method flue gas desulfurization ", the regeneration gas compressed action that produced when desulfurization solvent being regenerated with compressor, become high-temperature high-pressure overheat steam, and take this superheated steam as thermal source to regeneration tower bottoms heat and vaporize, thereby realized 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 exists compressor to contact 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 new energy-saving process.The present invention is from reducing the angle of plant energy consumption, raising efficiency, simple flow, reduction investment, realized to greatest extent the application advantage of heat pump in distillation field, heat pump techniques is combined with distillation, form adapt with distillation, simple, the small investment of technological process, energy-saving efficiency be up to 70% distillation new technology.
For achieving the above object, the present invention adopts following technical scheme:
A heat pump distillation new energy-saving process, is characterized in that: processing step is as follows:
Still liquid at the bottom of A, destilling tower is delivered to flash column, flash distillation in flash column;
The flash-off steam that B, flash distillation produce is sent into compressor, with compressor to flash-off steam compressed action;
C, the steam that compressor is exported are sent into destilling tower tower inner bottom part, form the required rising steam of distillation with the still liquid of vaporization, and the liquid countercurrent declining with tower top carries out mass-and heat-transfer, completes still-process;
The steam that discharge at still liquid after described part flash distillation and destilling tower top carries out heat exchange, after recovered steam heat, returns to flash column; Still liquid after remaining flash distillation carries out heat exchange with the feed liquid that enters destilling tower, reclaims after still liquid heat, then delivers to outside battery limit (BL) after water cooling.
The present invention is according to heat pump technical principle, and by the still liquid flash distillation at the bottom of destilling tower is formed to flash-off steam, the still liquid after flash distillation and the steam of tower top carry out sending to flash distillation after heat exchange again; Reclaim the flash steam after the heat of still liquid at the bottom of overhead vapours and tower simultaneously, after doing 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, thereby realized recycling when still liquid low temperature exhaust heat at the bottom of overhead vapours and tower.
The present invention can keep on the basis of former destilling tower operating condition completely, except system, is needing to consume more steam the starting period, only needs to consume a small amount of heating steam in the error-free running period.Therefore, the present invention compares with traditional distillating method, has the advantage that can significantly improve energy utilization rate, significantly reduce distillation energy consumption.For example, at doctor solution, absorb SO
2by distillation, from solution, reclaim SO in solution afterwards
2process in, in ammonia distillation process, adopting MEDA de-H from gas
2s, CO
2by distillation, from solution, reclaim H in solution afterwards
2s, CO
2process in, when adopting heat pump distillation flow process of the present invention to distill, its with adopt traditional distillating method to compare to can save energy more than 70%.
Preferably, the steam that discharge at described and destilling tower top carry out still liquid measure after the part flash distillation of heat exchange be enter destilling tower reduction of feed volume 1-10 doubly; The still liquid measure that described and the feed liquid that enters destilling tower are carried out after the remaining flash distillation of heat exchange is the 90-110% that enters the reduction of feed volume of destilling tower.
The steam that still liquid after described flash distillation and destilling tower are discharged carries out after heat exchange, and still liquid is warmed up to 95-120 ℃.
After the steam and the still liquid heat exchange after flash distillation that discharges at destilling tower of the present invention top, then carry out heat exchange with the feed liquid that enters destilling tower.The advantage of this order is that heat exchange area reduces, and at utmost reclaims heat.
Steam after described and feed liquid heat exchange after water-cooled, gas-liquid separation, gas recovery, liquid backflow is to destilling tower.
In step B of the present invention, the compression ratio of compressor is 1.8-4.
For realizing still-process, possess low energy consumption and efficient heat utilization efficiency, therefore with compressor during to flash-off steam compressed action, need consider the compression ratio of compressor, the present invention is set as 1.8-4 by compression ratio, this is mainly because too high compression ratio can cause compressor shaft power too high, energy-saving efficiency declines, and the too low energy-saving effect of compression ratio is not remarkable.
In described step B, with compressor, during to flash-off steam compressed action, the absolute pressure of compressor outlet steam is 0.12-0.3MPa, and temperature is 104-133 ℃.
From taking into account suitable compressor shaft power and suitable compressor outlet superheat steam temperature, the absolute pressure of setting flash steam compressor outlet superheated steam after compressor compression is 0.12-0.3MPa, temperature is 104-133 ℃, do not need by tower bottom reboiler and lean solution heat exchange, only need to be slightly high compared with the temperature and pressure of destilling tower bottom, the shaft power of compressor is low, and energy consumption is low.
Still liquid after described flash distillation with enter after the feed liquid heat exchange of destilling tower, feed liquid is warmed up to 75-90 ℃.
Described steps A, the absolute pressure of destilling tower overhead vapours is 0.1-0.2MPa, temperature is 90-124 ℃.
Described steps A, flash temperature is 75-120 ℃, pressure is 0.04-0.2 MPa.
Described step C, sends the steam of compressor output into destilling tower tower inner bottom part, and heating kettle liquid is to 103-124 ℃.
Beneficial effect of the present invention is:
1, the present invention can keep on the basis of former destilling tower operating condition completely, except system, is needing to consume more steam the starting period, only needs to consume a small amount of heating steam in the error-free running period.Therefore, the present invention compares with traditional distillating method, has the advantage that can significantly improve energy utilization rate, significantly reduce distillation energy consumption.For example, at doctor solution, absorb SO
2by distillation, from solution, reclaim SO in solution afterwards
2process in, in ammonia distillation process, adopting MEDA de-H from gas
2s, CO
2by distillation, from solution, reclaim H in solution afterwards
2s, CO
2process in, when adopting heat pump distillation flow process of the present invention to distill, its with adopt traditional distillating method to compare to can save energy more than 70%.
2, the present invention by compressor to destilling tower at the bottom of still liquid and overhead vapours reclaim the flash steam compressed action producing after heat, become high-temperature high-pressure overheat steam, and take this superheated steam and distillation tower reactor still liquid is heated and vaporized as thermal source, thereby realized the recycling to still liquid low temperature exhaust heat at the bottom of overhead vapours and tower, and with this, form there is high energy efficiency, the heat pump distillation flow process of low energy consumption, low operating cost feature.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 present invention directly enters in destilling tower by the high-temperature high-pressure overheat steam of compressor output at the bottom of tower, by the heat of still liquid and overhead vapours at the bottom of recovery tower, the required cooling water inflow of overhead vapours and common distil process comparison can significantly be reduced, thereby are conducive to further reduce the operating cost of distillation.
4, the present invention organically combines flash evaporation technology and heat pump techniques, for energy-saving distillation consumption reduction proposes a technology with novelty, has effectively solved the problem that traditional distil process steam consumption quantity is high, running cost is high;
5, at the bottom of the steam after compression is directly entered to destilling tower tower, do not need through the still liquid heat exchange at the bottom of reboiler and tower, vapor (steam) temperature and pressure after compression are lower, and heat transfer efficiency is high, and technological process is simple, easy to operate, small investment.Reboiler need to use when going into operation and normal operation period is the supplementary a small amount of heat of system.
6, the present invention utilizes flash evaporation technology not only to make the heat in still liquid be recycled, and after flash distillation, has further reduced the volatile components content in still liquid, by other supporting techniques of distillation provide strong guarantee.
accompanying drawing explanation
Fig. 1 is that technique of the present invention is for the heat pump distillation schematic flow sheet of residual coking ammonia water.
Fig. 2 is that technique of the present invention is prepared the heat pump distillation schematic flow sheet of concentrated ammonia liquor for residual coking ammonia water.
Fig. 3 is the heat pump distillation schematic flow sheet of technique of the present invention desulfurization solvent during for flue gas desulfurization.
In figure, be labeled as: 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.
The specific embodiment
Below in conjunction with the specific embodiment, essentiality content of the present invention is described in further detail.
Embodiment 1
A heat pump distillation new energy-saving process, processing step is as follows:
Still liquid at the bottom of A, destilling tower is delivered to flash column, flash distillation in flash column;
The flash-off steam that B, flash distillation produce is sent into compressor, with compressor to flash-off steam compressed action;
C, the steam that compressor is exported are sent into destilling tower tower inner bottom part, form the required rising steam of distillation with the still liquid of vaporization, and the liquid countercurrent declining with destilling tower top carries out mass-and heat-transfer, completes still-process;
The steam that discharge at still liquid after described part flash distillation and destilling tower top carries out heat exchange, after recovered steam heat, returns to flash column; Still liquid after remaining flash distillation carries out heat exchange with the feed liquid that enters destilling tower, reclaims after still liquid heat, then delivers to outside battery limit (BL) after water cooling.
Embodiment 2
A heat pump distillation new energy-saving process, processing step is as follows:
Still liquid at the bottom of A, destilling tower is delivered to flash column, flash distillation in flash column;
The flash-off steam that B, flash distillation produce is sent into compressor, with compressor to flash-off steam compressed action;
C, the steam that compressor is exported are sent into destilling tower tower inner bottom part, form the required rising steam of distillation with the still liquid of vaporization, and the liquid countercurrent declining with destilling tower top carries out mass-and heat-transfer, completes still-process;
The steam that discharge at still liquid after described part flash distillation and destilling tower top carries out heat exchange, after recovered steam heat, returns to flash column; Still liquid after remaining flash distillation carries out heat exchange with the feed liquid that enters destilling tower, reclaims after still liquid heat, then delivers to outside battery limit (BL) after water cooling.
It is 10 times of reduction of feed volume that enter destilling tower that the steam that discharge at described and destilling tower top carries out still liquid measure after the flash distillation of heat exchange; Described and the feed liquid that enters destilling tower carry out still liquid measure after the flash distillation of heat exchange be enter destilling tower reduction of feed volume 90%.
Outside battery limit (BL), refer to outside process system of the present invention, still liquid is delivered to other operations outside battery limit (BL) after water cooling.
Embodiment 3
A heat pump distillation new energy-saving process, processing step is as follows:
Still liquid at the bottom of A, destilling tower is delivered to flash column, flash distillation in flash column;
The flash-off steam that B, flash distillation produce is sent into compressor, with compressor to flash-off steam compressed action;
C, the steam that compressor is exported are sent into destilling tower tower inner bottom part, form the required rising steam of distillation with the still liquid of vaporization, and the liquid countercurrent declining with destilling tower top carries out mass-and heat-transfer, completes still-process;
The steam that discharge at still liquid after described part flash distillation and destilling tower top carries out heat exchange, after recovered steam heat, returns to flash column; Still liquid after remaining flash distillation carries out heat exchange with the feed liquid that enters destilling tower, reclaims after still liquid heat, then delivers to outside battery limit (BL) after water cooling.
It is 3 times of reduction of feed volume that enter destilling tower that the steam that discharge at described and destilling tower top carries out still liquid measure after the flash distillation of heat exchange; Described and the feed liquid that enters destilling tower carry out still liquid measure after the flash distillation of heat exchange be enter destilling tower reduction of feed volume 100%.
Embodiment 4
A heat pump distillation new energy-saving process, processing step is as follows:
Still liquid at the bottom of A, destilling tower is delivered to flash column, flash distillation in flash column;
The flash-off steam that B, flash distillation produce is sent into compressor, with compressor to flash-off steam compressed action;
C, the steam that compressor is exported are sent into destilling tower tower inner bottom part, form the required rising steam of distillation with the still liquid of vaporization, and the liquid countercurrent declining with destilling tower top carries out mass-and heat-transfer, completes still-process;
The steam that discharge at still liquid after described part flash distillation and destilling tower top carries out heat exchange, after recovered steam heat, returns to flash column; Still liquid after remaining flash distillation carries out heat exchange with the feed liquid that enters destilling tower, reclaims after still liquid heat, then delivers to outside battery limit (BL) after water cooling.
It is 1 times of reduction of feed volume that enters destilling tower that the steam that discharge at described and destilling tower top carries out still liquid measure after the flash distillation of heat exchange; Described and the feed liquid that enters destilling tower carry out still liquid measure after the flash distillation of heat exchange be enter destilling tower reduction of feed volume 110%.
Embodiment 5
A heat pump distillation new energy-saving process, processing step is as follows:
Still liquid at the bottom of A, destilling tower is delivered to flash column, flash distillation in flash column;
The flash-off steam that B, flash distillation produce is sent into compressor, with compressor to flash-off steam compressed action;
C, the steam that compressor is exported are sent into destilling tower tower inner bottom part, form the required rising steam of distillation with the still liquid of vaporization, and the liquid countercurrent declining with destilling tower top carries out mass-and heat-transfer, completes still-process;
The steam that discharge at still liquid after described part flash distillation and destilling tower top carries out heat exchange, after recovered steam heat, returns to flash column; Still liquid after remaining flash distillation carries out heat exchange with the feed liquid that enters destilling tower, reclaims after still liquid heat, then delivers to outside battery limit (BL) after water cooling.
It is 5 times of reduction of feed volume that enter destilling tower that the steam that discharge at described and destilling tower top carries out still liquid measure after the flash distillation of heat exchange; Described and the feed liquid that enters destilling tower carry out still liquid measure after the flash distillation of heat exchange be enter destilling tower reduction of feed volume 100%.
Embodiment 6
The present embodiment is substantially the same manner as Example 5, on this basis:
The steam that still liquid after described flash distillation and destilling tower are discharged carries out after heat exchange, and still liquid is warmed up to 90 ℃.
Embodiment 7
The present embodiment is substantially the same manner as Example 5, on this basis:
The steam that still liquid after described flash distillation and destilling tower are discharged carries out after heat exchange, and still liquid is warmed up to 100 ℃.
After the steam and the still liquid heat exchange after flash distillation that discharges at described destilling tower top, then carry out heat exchange with the feed liquid that enters destilling tower.
In described step B, the compression ratio of compressor is 1.8.
Embodiment 8
The present embodiment is substantially the same manner as Example 5, on this basis:
The steam that still liquid after described flash distillation and destilling tower are discharged carries out after heat exchange, and still liquid is warmed up to 110 ℃.
After the steam and the still liquid heat exchange after flash distillation that discharges at described destilling tower top, then carry out heat exchange with the feed liquid that enters destilling tower, the steam after heat exchange after water-cooled, gas-liquid separation, gas recovery, liquid backflow is to destilling tower.
In described step B, the compression ratio of compressor is 4.
In described step B, with compressor, during to flash-off steam compressed action, the absolute pressure of compressor outlet steam is 0.3MPa, and temperature is 133 ℃.
Embodiment 9
The present embodiment is substantially the same manner as Example 5, on this basis:
The steam that still liquid after described flash distillation and destilling tower are discharged carries out after heat exchange, and still liquid is warmed up to 101 ℃.
After the steam and the still liquid heat exchange after flash distillation that discharges at described destilling tower top, then carry out heat exchange with the feed liquid that enters destilling tower, the steam after heat exchange after water-cooled, gas-liquid separation, gas recovery, liquid backflow is to destilling tower.
In described step B, the compression ratio of compressor is 3.2.
In described step B, with compressor, during to flash-off steam compressed action, the absolute pressure of compressor outlet steam is 0.2MPa, and temperature is 115 ℃.
Still liquid after described flash distillation with enter after the feed liquid heat exchange of destilling tower, feed liquid is warmed up to 80 ℃.
Embodiment 10
The present embodiment is substantially the same manner as Example 5, on this basis:
The steam that still liquid after described flash distillation and destilling tower are discharged carries out after heat exchange, and still liquid is warmed up to 105 ℃.
After the steam and the still liquid heat exchange after flash distillation that discharges at described destilling tower top, then carry out heat exchange with the feed liquid that enters destilling tower, the steam after heat exchange after water-cooled, gas-liquid separation, gas recovery, liquid backflow is to destilling tower.
In described step B, the compression ratio of compressor is 2.5.
In described step B, with compressor, during to flash-off steam compressed action, the absolute pressure of compressor outlet steam is 0.15MPa, and temperature is 110 ℃.
Still liquid after described flash distillation with enter after the feed liquid heat exchange of destilling tower, feed liquid is warmed up to 85 ℃.
Described steps A, the absolute pressure of destilling tower overhead vapours is 0.13MPa, temperature is 106 ℃.
Embodiment 11
The present embodiment is substantially the same manner as Example 5, on this basis:
The steam that still liquid after described flash distillation and destilling tower are discharged carries out after heat exchange, and still liquid is warmed up to 115 ℃.
After the steam and the still liquid heat exchange after flash distillation that discharges at described destilling tower top, then carry out heat exchange with the feed liquid that enters destilling tower, the steam after heat exchange after water-cooled, gas-liquid separation, gas recovery, liquid backflow is to destilling tower.
In described step B, the compression ratio of compressor is 2.
In described step B, with compressor, during to flash-off steam compressed action, the absolute pressure of compressor outlet steam is 0.2MPa, and temperature is 120 ℃.
Still liquid after described flash distillation with enter after the feed liquid heat exchange of destilling tower, feed liquid is warmed up to 85 ℃.
Described steps A, the absolute pressure of destilling tower overhead vapours is 0.18MPa, temperature is 115 ℃.
Described steps A, flash temperature is 110 ℃, pressure is 0.1MPa.
Embodiment 12
The present embodiment is substantially the same manner as Example 5, on this basis:
The steam that still liquid after described flash distillation and destilling tower are discharged carries out after heat exchange, and still liquid is warmed up to 95 ℃.
After the steam and the still liquid heat exchange after flash distillation that discharges at described destilling tower top, then carry out heat exchange with the feed liquid that enters destilling tower, the steam after heat exchange after water-cooled, gas-liquid separation, gas recovery, liquid backflow is to destilling tower.
In described step B, the compression ratio of compressor is 3.
In described step B, with compressor, during to flash-off steam compressed action, the absolute pressure of compressor outlet steam is 0.12MPa, and temperature is 104 ℃.
Still liquid after described flash distillation with enter after the feed liquid heat exchange of destilling tower, feed liquid is warmed up to 75 ℃.
Described steps A, the absolute pressure of destilling tower overhead vapours is 0.1MPa, temperature is 90 ℃.
Described steps A, flash temperature is 75 ℃, pressure is 0.04 MPa.
Described step C, sends the steam of compressor output into destilling tower tower inner bottom part, heating kettle liquid to 103 ℃.
Embodiment 13
The present embodiment is substantially the same manner as Example 5, on this basis:
The steam that still liquid after described flash distillation and destilling tower are discharged carries out after heat exchange, and still liquid is warmed up to 115 ℃.
After the steam and the still liquid heat exchange after flash distillation that discharges at described destilling tower top, then carry out heat exchange with the feed liquid that enters destilling tower, the steam after heat exchange after water-cooled, gas-liquid separation, gas recovery, liquid backflow is to destilling tower.
In described step B, the compression ratio of compressor is 2.2.
In described step B, with compressor, during to flash-off steam compressed action, the absolute pressure of compressor outlet steam is 0.3MPa, and temperature is 133 ℃.
Still liquid after described flash distillation with enter after the feed liquid heat exchange of destilling tower, feed liquid is warmed up to 90 ℃.
Described steps A, the absolute pressure of destilling tower overhead vapours is 0.2MPa, temperature is 118 ℃.
Described steps A, flash temperature is 110 ℃, pressure is 0.15 MPa.
Described step C, sends the steam of compressor output into destilling tower tower inner bottom part, heating kettle liquid to 124 ℃.
Embodiment 14
The present embodiment is substantially the same manner as Example 5, on this basis:
The steam that still liquid after described flash distillation and destilling tower are discharged carries out after heat exchange, and still liquid is warmed up to 105 ℃.
After the steam and the still liquid heat exchange after flash distillation that discharges at described destilling tower top, then carry out heat exchange with the feed liquid that enters destilling tower, the steam after heat exchange after water-cooled, gas-liquid separation, gas recovery, liquid backflow is to destilling tower.
In described step B, the compression ratio of compressor is 3.2.
In described step B, with compressor, during to flash-off steam compressed action, the absolute pressure of compressor outlet steam is 0.15MPa, and temperature is 111 ℃.
Still liquid after described flash distillation with enter after the feed liquid heat exchange of destilling tower, feed liquid is warmed up to 82 ℃.
Described steps A, the absolute pressure of destilling tower overhead vapours is 0.12MPa, temperature is 95 ℃.
Described steps A, flash temperature is 80 ℃, pressure is 0.05 MPa.
Described step C, sends the steam of compressor output into destilling tower tower inner bottom part, heating kettle liquid to 108 ℃.
Embodiment 15
The present embodiment is substantially the same manner as Example 3, on this basis:
The steam that still liquid after described flash distillation and destilling tower are discharged carries out after heat exchange, and still liquid is warmed up to 102 ℃.
After the steam and the still liquid heat exchange after flash distillation that discharges at described destilling tower top, then carry out heat exchange with the feed liquid that enters destilling tower, the steam after heat exchange after water-cooled, gas-liquid separation, gas recovery, liquid backflow is to destilling tower.
In described step B, the compression ratio of compressor is 2.6.
In described step B, with compressor, during to flash-off steam compressed action, the absolute pressure of compressor outlet steam is 0.12MPa, and temperature is 104 ℃.
Still liquid after described flash distillation with enter after the feed liquid heat exchange of destilling tower, feed liquid is warmed up to 90 ℃.
Described steps A, the absolute pressure of destilling tower overhead vapours is 0.10MPa, temperature is 99 ℃.
Described steps A, flash temperature is 82 ℃, pressure is 0.052MPa.
Described step C, sends the steam of compressor output into destilling tower tower inner bottom part, heating kettle liquid to 106 ℃.
Embodiment 16
While take the solvent cycle absorption method flue gas desulfurization of steel works sintering flue gas, the heat pump distillation of desulfurization solvent is example (see figure 3).
From desulfurizing tower, contain SO
2desulfurization solvent (rich solution) through poor rich liquid heat exchanger with from still liquid (lean solution) heat exchange of flash column, be heated to 90 ℃;
The 0.19MPa(absolute pressure producing from distillation tower top), after the steam of the 118 ℃ lean solution heat exchange with flash column, then with rich or poor liquid heat exchange after rich solution heat exchange after, steam arrives 40 ℃-50 ℃ of technological requirement by water cooling, rich solution is sent into destilling tower.
Rich solution on inner-tower filling material with tower reactor in the steam that rises carry out counter current contacting, by heating, stripping effect, distill out wherein contained SO
2.Gained desulfurization solvent lean solution after distillation (distillation tower reactor night) is delivered to flash column from destilling tower, by flash distillation, form flash steam, flash steam is delivered to destilling tower inner bottom part after compressor compresses, and the steam forming with the lean solution of partly vaporizing forms the rising steam 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, after water-cooled cooling to 45 ℃, send desulfurization section to recycle.
The 0.19MPa(absolute pressure that distillation tower top produces), the steam of 118 ℃, the lean solution heat exchange coming with flash column, then with rich or poor liquid heat exchange after rich solution heat exchange after, the lean solution that last flash column comes and the steam heat-exchanging to 116 ℃ of distillation tower top, turn back to flash column.
Flash column internal pressure is 0.07MPa, and flash steam temperature is 89 ℃, 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 ℃.The superheated steam of compressor output is delivered to the bottom in destilling tower, in destilling tower, lean solution temperature is heated to 123 ℃, forms the rising steam in destilling tower together with the part lean solution of vaporizing.
Embodiment 17
Take residual coking ammonia water heat pump distillation as example (see figure 1).
The present embodiment is chosen residual coking ammonia water, and treating capacity is 60t/h, containing ammonia concentration 6000 mg/L.After the distilled ammonia wastewater heat exchange of the remained ammonia of sending here from battery limit (BL) and flash column, enter ammonia distillation tower, ammonia distillation tower top pressure is 0.12MPa(absolute pressure), tower top temperature is 105 ℃, tower bottom pressure is 0.14MPa(absolute pressure), column bottom temperature is 109 ℃.
Distilled ammonia wastewater at the bottom of ammonia distillation tower is delivered to flash column, distilled ammonia wastewater after flash distillation returns to flash column after delivering to ammonia distillation tower top and tower top ammonia steam heat-exchanging, temperature after ammonia steam heat-exchanging is 95 ℃-102 ℃ and delivers to lower operation (meeting different technological requirements), if produce concentrated ammonia liquor, ammonia steam again with distilled ammonia wastewater heat exchange after remained ammonia heat exchange, finally by crossing water cooling, obtain concentrated ammonia liquor.Distilled ammonia wastewater is flash distillation in flash column, and flashing pressure is 0.05 MPa, and temperature is 81 ℃, flash steam by vapour compression machine be forced into 0.18MPa, temperature is delivered to ammonia still inner bottom part after being increased to 148 ° of C, as the thermal source of ammonia distillation.Meanwhile, the part waste water in flash column, through with remained ammonia heat exchange, water cooling after enter lower operation.Ammonia distillation tower goes into operation and need to adopt steam, can directly the live steam outside battery limit (BL) directly be passed in ammonia distillation tower, also can arrange and in a reboiler, pass into live steam indirect distilled ammonia wastewater.
Adopt as above technology, its processed waste water reduces, and processes ton remained ammonia by originally needing the steam 175Kg of 0.6MPa to be reduced to below 50Kg.
Embodiment 18
Take residual coking ammonia water heat pump distillation as example (see figure 2).
The present embodiment is chosen coking ammonia water, and treating capacity is 80t/h, containing ammonia concentration 4000 mg/L.After the distilled ammonia wastewater heat exchange of the ammoniacal liquor of sending here from battery limit (BL) and flash column, enter ammoniacal liquor ammonia still, ammoniacal liquor ammonia still pressure on top surface is 0.13MPa(absolute pressure), tower top temperature is 107 ℃, tower bottom pressure is 0.15MPa(absolute pressure), column bottom temperature is 110 ℃.
Distilled ammonia wastewater at the bottom of ammoniacal liquor ammonia still is delivered to flash column, distilled ammonia wastewater after flash distillation returns to flash column after delivering to ammoniacal liquor ammonia still process tower top and tower top ammonia steam heat-exchanging, with distilled ammonia wastewater amount after the vapor heated flash distillation of ammonia be 5 times of ammonia vol that enter ammonia still, after ammonia steam heat-exchanging, again with the ammonia still process ammoniacal liquor heat exchange that enters ammonia still, ammonia, through water cooling to 50 ℃, obtains concentrated ammonia liquor.
Distilled ammonia wastewater is flash distillation in flash column, and flashing pressure is 0.07 MPa, and temperature is 90 ℃, flash steam by vapour compression machine be forced into 0.15MPa, temperature is delivered to ammonia still inner bottom part after being increased to 135 ° of C, as the thermal source of ammonia distillation.Meanwhile, the part waste water in flash column, through with ammoniacal liquor heat exchange, water cooling after enter lower operation.Ammoniacal liquor ammonia still goes into operation and need to adopt steam, can directly the live steam outside battery limit (BL) directly be passed in ammoniacal liquor ammonia still, also can arrange and in a reboiler, pass into live steam indirect distilled ammonia wastewater.
Adopt as above technology, its processed waste water reduces, and processes ton ammoniacal liquor by originally needing the steam 175Kg of 0.6MPa to be reduced to below 40Kg.
Embodiment 19
With the de-H of Gas Purification Factory MEDA desulfuration solution
2s, the separated H of heat pump distillation
2s is example.
Gas Purification Factory adopts the amine desulphurization solvents such as MEDA from natural gas, to remove H
2s, CO
2, absorbed H
2s, CO
2rich solution Deng sour gas, rich solution after flash distillation, by being pumped into lean solution heat exchange to 65 after heat exchanger and flash distillation ℃-90 ℃, rich solution again with lean solution heat exchange after flash distillation after overhead vapours heat exchange to 100 ℃-110 ℃ after enter destilling tower, lean solution at the bottom of destilling tower is delivered to flash column, flash steam after flash distillation is directly sent into destilling tower inner bottom part after by compressor compresses, and the lean solution part after flash distillation is returned to flash column after delivering to the steam heat-exchanging that tower top and destilling tower come again; Part lean solution is delivered to after heat exchanger and rich solution heat exchange after water cooling to 40 ℃-50 ℃ again and is delivered to absorption tower.After the lean solution heat exchange of the steam of tower top after flash distillation again with rich solution heat exchange, finally by water cooling to 30 ℃-50 ℃, obtain concentration higher containing H
2s, CO
2deng sour gas, deliver to lower operation.
Lean solution flashing pressure is controlled 0.05 MPa-0.11 MPa, temperature is 81 ℃-101 ℃, flash steam by vapour compression machine be forced into 0.14MPa-0.24MPa, temperature is delivered to destilling tower inner bottom part after being increased to 120 ° of C-180 ° of C, as the thermal source of the amine desulphurization solvent such as MEDA distillation.
Embodiment 20
With coke-oven gas desulfurizer, adopt SUIFIBAN method to remove coke-stove gas H
2s, HCN and CO
2, the de-separated H of heat pump distillation that adopts of desulfuration solution
2s, HCN and CO
2for example.
SUIFIBAN technique by desulfuration and decyanation with 15% MEA as desulfurizing agent, under cryogenic conditions, absorb the H in coke-stove gas
2s, HCN and CO
2, then parse the sour gas in solution with steam distillation.
Absorbed H
2s, HCN, CO
2rich solution Deng sour gas, by being pumped into lean solution heat exchange to 65 after heat exchanger and flash distillation ℃-90 ℃, rich solution again with lean solution heat exchange after flash distillation after overhead vapours heat exchange to 100 ℃-110 ℃ after enter destilling tower, lean solution at the bottom of destilling tower is delivered to flash column, flash steam after flash distillation is directly sent into destilling tower inner bottom part after by compressor compresses, and the lean solution part after flash distillation is returned to flash column after delivering to the steam heat-exchanging that tower top and destilling tower come again; Part lean solution is delivered to after heat exchanger and rich solution heat exchange after water cooling to 25 ℃-28 ℃ again and is delivered to absorption tower.After the lean solution heat exchange of the steam of tower top after flash distillation again with rich solution heat exchange, finally by water cooling to 30 ℃-50 ℃, obtain concentration higher containing H
2s, CO
2deng sour gas, deliver to lower operation.
Lean solution flashing pressure is controlled 0.075 MPa-0.09 MPa, temperature is 91 ℃-98 ℃, flash steam by vapour compression machine be forced into 0.14MPa-0.18MPa, temperature is delivered to destilling tower inner bottom part after being increased to 120 ° of C-156 ° of C, as the thermal source of the amine desulphurization solvent such as MEDA distillation.
Embodiment 21
Using the aqueous solution of hot wet chemical, ethanolamines as absorbent or using other aqueous solution as absorbent, from gas, absorbing CO
2after adopt again heat pump distillation mode to obtain high-purity CO
2for example, and the present invention will be described in conjunction with Fig. 3.
Using the aqueous solution of hot wet chemical, ethanolamines as absorbent or using other aqueous solution as absorbent, from gas, absorbing CO
2after rich solution, by being pumped into lean solution heat exchange to 75 after heat exchanger and flash distillation ℃-90 ℃, rich solution again with lean solution heat exchange after flash distillation after overhead vapours heat exchange to 102 ℃-106 ℃ after enter destilling tower, lean solution at the bottom of destilling tower is delivered to flash column, flash steam after flash distillation is directly sent into destilling tower inner bottom part after by compressor compresses, and the lean solution part after flash distillation is returned to flash column after delivering to the steam heat-exchanging that tower top and destilling tower come again; Part lean solution is delivered to after heat exchanger and rich solution heat exchange after water cooling to 30 ℃-50 ℃ again and is delivered to absorption tower.After the lean solution heat exchange of the steam of tower top after flash distillation again with rich solution heat exchange, finally by water cooling to 30 ℃-50 ℃, high concentration CO
2gas, delivers to lower operation.
Lean solution flashing pressure is controlled 0.065 MPa-0.11 MPa, and temperature is 88 ℃-102 ℃, flash steam by vapour compression machine be forced into 0.15MPa-0.22MPa, temperature is delivered to destilling tower inner bottom part after being increased to 115 ° of C-190 ° of C, as the thermal source of decarbonizing solution distillation.
As can be seen here, a kind of heat pump distillation flow process of the present invention is compared with conventional non-heat pump distillation flow process, possesses the advantage of obvious low energy consumption, high energy efficiency, low operating cost.Compare with other heat pump distillation flow processs that to have heat recovery efficiency high, the high-temperature steam of compression does not need by reboiler indirect, and vapor (steam) temperature and pressure after compression are lower, the low advantage of power consumption of compressor.
Claims (11)
1. a heat pump distillation new energy-saving process, is characterized in that: processing step is as follows:
Still liquid at the bottom of A, destilling tower is delivered to flash column, flash distillation in flash column;
The flash-off steam that B, flash distillation produce is sent into compressor, with compressor to flash-off steam compressed action;
C, the steam that compressor is exported are sent into destilling tower tower inner bottom part, form the required rising steam of distillation with the still liquid of vaporization, and the liquid countercurrent declining with destilling tower top carries out mass-and heat-transfer, completes still-process;
The steam that discharge at still liquid after described part flash distillation and destilling tower top carries out heat exchange, after recovered steam heat, returns to flash column; Still liquid after remaining flash distillation carries out heat exchange with the feed liquid that enters destilling tower, reclaims after still liquid heat, then delivers to outside battery limit (BL) after water cooling.
2. a kind of heat pump distillation new energy-saving process according to claim 1, is characterized in that: described steam of discharging with destilling tower top carry out still liquid measure after the flash distillation of heat exchange be enter destilling tower reduction of feed volume 1-10 doubly; The still liquid measure that described and the feed liquid that enters destilling tower are carried out after the flash distillation of heat exchange is the 90-110% that enters the reduction of feed volume of destilling tower.
3. a kind of heat pump distillation new energy-saving process according to claim 1, is characterized in that: the steam that the still liquid after described flash distillation and destilling tower are discharged carries out after heat exchange, and still liquid is warmed up to 95-120 ℃.
4. a kind of heat pump distillation new energy-saving process according to claim 1, is characterized in that: after the steam and the still liquid heat exchange after flash distillation that discharges at described destilling tower top, then carry out heat exchange with the feed liquid that enters destilling tower.
5. a kind of heat pump distillation new energy-saving process according to claim 4, is characterized in that: the steam after described and feed liquid heat exchange after water-cooled, gas-liquid separation, gas recovery, liquid backflow is to destilling tower.
6. a kind of heat pump distillation new energy-saving process according to claim 1, is characterized in that: in described step B, the compression ratio of compressor is 1.8-4.
7. a kind of heat pump distillation new energy-saving process according to claim 1, is characterized in that: in described step B, with compressor, during to flash-off steam compressed action, the absolute pressure of compressor outlet steam is 0.12-0.3MPa, and temperature is 104-133 ℃.
8. a kind of heat pump distillation new energy-saving process according to claim 1, is characterized in that: the still liquid after described flash distillation with enter after the feed liquid heat exchange of destilling tower, feed liquid is warmed up to 75-90 ℃.
9. a kind of heat pump distillation new energy-saving process according to claim 1, is characterized in that: described steps A, and the absolute pressure of destilling tower overhead vapours is 0.1-0.2MPa, temperature is 90-124 ℃.
10. a kind of heat pump distillation new energy-saving process according to claim 1, is characterized in that: described steps A, and flash temperature is 75-120 ℃, pressure is 0.04-0.2 MPa.
11. a kind of heat pump distillation new energy-saving process according to claim 1, is characterized in that: described step C, the steam of compressor output is sent into destilling tower tower inner bottom part, and heating kettle liquid is to 103-124 ℃.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105056561A (en) * | 2015-07-24 | 2015-11-18 | 河北新欣园能源股份有限公司 | Rectification energy-saving device and energy-saving process therefor |
| CN106542965A (en) * | 2016-11-07 | 2017-03-29 | 青岛科技大学 | The method of MAS tower reactor flash separation methanol |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60168582A (en) * | 1984-02-14 | 1985-09-02 | Mitsui Eng & Shipbuild Co Ltd | Steam compression type water distillation apparatus |
| CN102190341A (en) * | 2010-03-09 | 2011-09-21 | 天华化工机械及自动化研究设计院 | Stripping ammonia-removing method based on flash evaporation and heat pump technologies |
| CN102807259A (en) * | 2012-08-03 | 2012-12-05 | 济钢集团有限公司 | Heat pump distillation system of residual ammonia water |
-
2014
- 2014-07-11 CN CN201410328909.XA patent/CN104056461B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60168582A (en) * | 1984-02-14 | 1985-09-02 | Mitsui Eng & Shipbuild Co Ltd | Steam compression type water distillation apparatus |
| CN102190341A (en) * | 2010-03-09 | 2011-09-21 | 天华化工机械及自动化研究设计院 | Stripping ammonia-removing method based on flash evaporation and heat pump technologies |
| CN102807259A (en) * | 2012-08-03 | 2012-12-05 | 济钢集团有限公司 | Heat pump distillation system of residual ammonia water |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105056561A (en) * | 2015-07-24 | 2015-11-18 | 河北新欣园能源股份有限公司 | Rectification energy-saving device and energy-saving process therefor |
| CN106542965A (en) * | 2016-11-07 | 2017-03-29 | 青岛科技大学 | The method of MAS tower reactor flash separation methanol |
| CN106542965B (en) * | 2016-11-07 | 2019-07-16 | 青岛科技大学 | The method of low carbon mixed alcohol tower reactor flash separation methanol |
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