CN202620989U - Separation system for mixed gas of ammonia and carbon dioxide - Google Patents
Separation system for mixed gas of ammonia and carbon dioxide Download PDFInfo
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- CN202620989U CN202620989U CN2012202778517U CN201220277851U CN202620989U CN 202620989 U CN202620989 U CN 202620989U CN 2012202778517 U CN2012202778517 U CN 2012202778517U CN 201220277851 U CN201220277851 U CN 201220277851U CN 202620989 U CN202620989 U CN 202620989U
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Abstract
The utility model provides a separation system for the mixed gas of ammonia and carbon dioxide. The system is used for compressing the mixed gas of ammonia and carbon dioxide at first, conveying the mixed gas in a carbon dioxide separation tower after the pressure rises to 15-25 bar, and then sequentially conveying the mixed gas in a water separation tower and an ammonia separation tower; and the system with the arrangement has the advantage that the electric energy consumed by compressed tail gas is converted to the enthalpy of the tail gas, and in the case that the ammonia in the tail gas is absorbed in the carbon separation tower, lots of heat released is effectively utilized; simultaneously, dilute ammonia-carbon aqueous solution is separated from the side line of the water separation tower by the separation system provided by the utility model, thus the load of the water separation tower is greatly reduced and energy consumption is also reduced. Additionally, compression for the mixed gas is divided into a plurality of sections by the separation system provided by the utility model, and inter-section cooling is realized by adopting a direct liquid-spray cooling method instead of a traditional indirect water cooling method; and the separation system has the advantage that sensible heat is converted to latent heat, and the total enthalpy value of a material flow keeps invariable. The separation system provided by the utility model has the fourth advantage that an air cooler is used for replacing a cooler which takes circulation cooling water as a cooling medium, thus energy consumption is saved.
Description
Technical field
The utility model belongs to the gas separation field, is specifically related to a kind of piece-rate system that is used for ammonia and carbon dioxide gas mixture.
Background technology
Can produce the mist that contains ammonia, carbon dioxide in a large number at urea synthesis and in,, will separate gas usually in order further to utilize ammonia and the carbon dioxide in the gas with the process of urea production of melamine.
The phase equilibrium relationship of ammonia, carbon dioxide, water ternary system is very complicated, and it does not follow Raoult's law, can only represent with the phasor of making according to experimental data.Accompanying drawing one is the sketch map of the isobaric phasor of this system.Leg-of-mutton three summits are represented ammonia, carbon dioxide and water respectively, are called ammonia angle, carbon angle, Shui Jiao respectively.The curve III is called liquid phase top crestal line, represents azeotropic mixture.It is the ammonia rectification zone that the upper left zone of curve III is called the I district, and it is the carbon dioxide rectification zone that the bottom-right zone of curve III is called the II district.The dotted line IV is called the crystallization line, and its right side, top are the gas-liquid-solid three-phase coexistence.When the ammonia carbon aqueous solution that is positioned at the I district when composition distilled, along with constantly steaming of ammonia, liquid phase top crestal line is shifted to and arrived at last to the composition of residue liquid phase; When the ammonia carbon aqueous solution that is positioned at the II district when composition distilled, along with constantly steaming of carbon dioxide gas, liquid phase top crestal line is also shifted to and arrived at last to the composition of remaining liquid phase; The ammonia carbon aqueous solution that composition is positioned on the crestal line III of liquid phase top distills, and the ammonia of gas phase and liquid phase is identical with the mass ratio of carbon dioxide, promptly can't carry out ammonia carbon and separate.If continue distillation, then crestal line moves to the water angle liquid phase composition along the liquid phase top, till liquid phase becomes pure water.
The separation method of known ammonia carbon mix such as dilution method (dilution process), differential pressure method (pressure differential process) etc.; All the isobaric phasor with above-mentioned ammonia, carbon dioxide, water ternary system is a theoretical foundation, and these methods all comprise following three parts: in the ammonia separating part of the I district of phasor operation, the carbon dioxide separation part in the operation of the II district of phasor, the desorb part (separated form water part) of on the crestal line III of the liquid phase top of phasor, operating.Separation order for ammonia and carbon dioxide; When the composition of the ammonia carbon aqueous solution is positioned at the ammonia rectification zone of phasor; Then this mixture at first is introduced into the ammonia Disengagement zone and separates; Disclose the method for separating ammonia and carbon dioxide like american documentation literature US4163648, wherein a kind of method comprises: the ammonia knockout tower is sent mist in (1), and isolated ammonia is shifted out; (2) will after step (1) is separated, send into the carbon dioxide separation tower by the remaining liquid that contains ammonia, carbon dioxide and water, isolated carbon dioxide will be shifted out; (3) will after step (2) is separated, send into Analytic Tower by the remaining liquid that contains ammonia, carbon dioxide and water, and the gas that contains ammonia, carbon dioxide and water vapour that parses returned the ammonia knockout tower again separate.In the said method, the bottom operating temperature of ammonia knockout tower is 60-170 ℃, and the bottom operating temperature of carbon dioxide separation tower is 75-200 ℃, and the operating pressure of carbon dioxide separation tower is no more than the twice of ammonia knockout tower.
Except carrying out the separation processes the above-mentioned ammonia Disengagement zone that at first gets into, if when the composition of the ammonia carbon aqueous solution is positioned at the carbon rectification zone of phasor, then this mixture at first is introduced into the carbon knockout tower and separates.A kind of method of utilizing melamine tail gas to reclaim carbon dioxide and liquefied ammonia is disclosed like Chinese patent document CN101862577A; Comprise: (1) is sent into the carbon dioxide separation tower with the ammonia carbon mix with aqueous solution form; Use the steam indirect at the bottom of the tower; Cat head is isolated the carbon dioxide that contains 5% steam, obtains decarburization ammoniacal liquor at the bottom of the tower; (2) above-mentioned decarburization ammoniacal liquor is got into water separation column, thoroughly resolve through heating, what obtain at the bottom of the tower separates bleed, through cooling, is sent to the absorption water of above-mentioned Melamine Production device as ammonia carbon mist, and cat head obtains separating gassing; (3) to separate gassing dry through rectifying in the ammonia rectifying column with above-mentioned, obtains pure ammonia gas from cat head, and the isolated ammonia spirit that contains carbon dioxide returns the carbon dioxide separation tower again at the bottom of the tower.
But the defective that the method that ammonia carbon separates in the above-mentioned prior art exists is that said method needs the steam of labor to heat at the carbon dioxide separation tower, and energy consumption is bigger.Especially for earlier ammonia carbon mist water being absorbed in the prior art; When sending into the carbon dioxide separation tower with aqueous solution form again,, need first consumed energy that the heat of solution of ammonia and carbon dioxide is shifted out in order to promote the absorption of ammonia carbon; Behind ammonia carbon aqueous solution entering carbon dioxide separation tower; Also need consumed energy that carbon dioxide is steamed from liquid phase, this has just further increased the energy consumption of piece-rate system, has reduced the economic benefit of separating technology again.
Summary of the invention
The carbon dioxide separation tower needs the steam of labor to heat in the prior art in order to solve; Energy consumption is bigger; Especially for elder generation in the prior art ammonia carbon mist water is absorbed, when sending into the carbon dioxide separation tower with aqueous solution form again, in order to promote the absorption of ammonia carbon mist; Need first consumed energy that the heat of solution of ammonia and carbon dioxide is shifted out; Behind ammonia carbon aqueous solution entering carbon dioxide separation tower, also need again consumed energy that carbon dioxide is steamed from liquid phase, further increase the problem of piece-rate system energy consumption.The utility model provides a kind of can reduce steam consumption significantly, thereby reduces the ammonia of system energy consumption and the piece-rate system of carbon dioxide.
The technical scheme of the piece-rate system of described ammonia of the utility model and carbon dioxide is:
A kind of piece-rate system that is used for ammonia and carbon dioxide gas mixture comprises:
The carbon dioxide separation tower;
Be connected with water separation column with said carbon dioxide separation tower;
Be connected with the ammonia knockout tower with said water separation column;
Said system also is provided with the gas compressing apparatus that said ammonia and carbon dioxide gas mixture are compressed, and the outlet of said gas compressing apparatus is connected with said carbon dioxide separation tower.
The ammonia of said gas compressing apparatus outlet and the pressure of carbon dioxide gas mixture are 15-25bar.
The operating pressure of said carbon dioxide separation Tata still is 15-25bar, and operating temperature is 155-186 ℃.
The operating pressure of said carbon dioxide separation Tata still is 18bar, and operating temperature is 165-171 ℃.
The operating pressure of said ammonia knockout tower is 2-18bar, and tower still operating temperature is 60-140 ℃.
The operating pressure of said ammonia knockout tower is 2-4bar, and tower still operating temperature is 60-85 ℃.
Said gas compressing apparatus is the multistage gas compressing apparatus.
The top of said water separation column is provided with reflux condenser, and said reflux condenser is an air cooler.
The bottom of said ammonia knockout tower and/or middle part are provided with circulating pump and recirculation cooler.
The recirculation cooler of said ammonia knockout tower is an air cooler.
The middle part of said water separation column is provided with side line extraction pump.
The advantage of the piece-rate system of described ammonia of the utility model and carbon dioxide gas mixture is:
(1) the described piece-rate system that is used for ammonia and carbon dioxide gas mixture of the utility model is provided with compression set ammonia and carbon dioxide gas mixture is carried out one section or multistage compression, makes pressure rise to 15 ~ 25bar.Conventional method is that first water absorbs ammonia carbon mist, generates the ammonia carbon aqueous solution.Then the ammonia carbon aqueous solution is sent into carbon knockout tower separating carbon dioxide, or send into the ammonia knockout tower and separate ammonia.When water absorbed ammonia carbon gaseous mixture, a large amount of heats of solution not only were not used, and also will heat of solution be shifted out with a large amount of recirculated cooling waters; And send into carbon knockout tower separating carbon dioxide when the ammonia carbon aqueous solution, or when sending into the ammonia knockout tower and separating ammonia, consume significant amount of energy again and remove to heat the ammonia carbon aqueous solution, so that carbon dioxide or ammonia are desorbed.
The utility model further limits to be sent into the carbon knockout tower with the compression of ammonia carbon gaseous mixture to 15 ~ 25bar and removes separating carbon dioxide.Its advantage is: in the carbon knockout tower, carbon dioxide has been a gaseous state, does not need desorb; A large amount of heats of emitting when the ammonia of gaseous state is absorbed by water are directly absorbed by the water that flows from top to bottom in the tower or the ammonia carbon aqueous solution, thereby have significantly reduced the steam consumption quantity of reboiler; The electric energy that compressor consumed almost all is converted into the interior ability (enthalpy) of tail gas; Tail gas after the compression is compared with the preceding tail gas of compression; The value added of its enthalpy approximates the electric energy that compressor consumes; That is: the electric energy that compressor consumed is loss not, but is brought into the carbon knockout tower, has obtained utilization.
(2) the described piece-rate system that is used for ammonia and carbon dioxide gas mixture of the utility model is carried out the segmentation compression to ammonia and carbon dioxide gas mixture, and in intersegmental use hydrojet cooling method said mist is cooled off.Comparing its advantage with indirect cooling method habitual in the prior art is; The sensible heat of Compressed Gas is converted into latent heat; Total enthalpy of material remains unchanged, i.e. not loss of energy in the temperature-fall period is if adopt indirect cooling method; Then not only the enthalpy of Compressed Gas reduces, and also will consume extra energy and carry cooling medium.
(3) the described piece-rate system that is used for ammonia and carbon dioxide gas mixture of the utility model, the operating pressure of said carbon dioxide separation tower is 15-25bar, operating temperature is 160-190 ℃.The utility model is a foundation with the isobaric phasor of ammonia, carbon dioxide, water, has provided optimal operation conditions, and operation can improve the separative efficiency of carbon dioxide separation tower, the energy consumption of reduction operating system in above-mentioned pressure and temperature scope.The operating pressure that the utility model is provided with the carbon dioxide separation tower is 15-25bar.Pressure is bigger to the shape affects of top crestal line in the isobaric phasor of NH3-CO2-H2O ternary; The lower semisection of the high more top of pressure crestal line is more to left avertence; The ratio of ammonia and carbon dioxide that is positioned at the liquid phase on this top, place crestal line is also big more; But when pressure surpasses 25bar continuation rising, more and more littler to the trend of left avertence, so the operating pressure of carbon dioxide separation tower is advisable with 15-25bar.
The content that the utility model is provided with ammonia in the operating temperature control carbon dioxide of carbon dioxide separation column overhead is lower than 50pm.
In addition, the utility model also operating pressure of further preferred said carbon dioxide separation tower is 18bar, and the operating temperature at the bottom of the said carbon dioxide separation Tata is 165-171 ℃, and the operating temperature of cat head is 70-90 ℃.When carbon dioxide separation tower operating pressure is 18bar, in suitable operating space, to operate, tower still temperature is between 165-171 ℃.If temperature is lower than 165 ℃, then the liquid phase ammonia carbon ratio diminishes, and the carbon dioxide that separative efficiency descends, in system, circulates increases, and energy consumption increases; If temperature continue to raise from 171 ℃, ammonia content reduces rapidly in the liquid phase, water content increases rapidly, but because the total amount of the ammonia of discharging from the carbon dioxide separation tower bottom is constant, this means that the internal circulating load of water increases greatly, thereby energy consumption increases greatly also.
(4) the described piece-rate system that is used for ammonia and carbon dioxide gas mixture of the utility model, the operating pressure of said ammonia knockout tower is 2-18bar.Tower still operating temperature is 60-140 ℃, in this scope, operates, and the ammonia of liquid phase and the mass ratio of carbon dioxide are less; The separative efficiency of ammonia tower is high, and the suitable safe distance of the fusing point of liquid phase boiling point and aminoquinoxaline (crystallization line IV) maintenance, can avoid generating knot. crystalline substance; The influence operation; Therefore the ammonia tower is operated in this zone, and not only stable operation, and energy consumption is also lower.
(5) the described piece-rate system that is used for ammonia and carbon dioxide gas mixture of the utility model; The aqueous solution of separating at the bottom of the tower of said water separation column is as the loop solution the carbon dioxide separation tower; The aqueous solution of separating at the bottom of the tower of said water separation column is sent into from the top of said carbon dioxide separation tower; Reason is to send into the purity requirement of water of carbon dioxide separation top of tower than higher (should≤0.2% like its ammonia content); So that make the content≤50pm of ammonia in the carbon dioxide that the carbon dioxide separation cat head steams; And the aqueous solution of separating at the bottom of the tower of said water separation column contains ammonia hardly, therefore is suitable for the recirculated water as the carbon dioxide separation top of tower.
(6) the described piece-rate system that is used for ammonia and carbon dioxide gas mixture of the utility model; As the loop solution the carbon dioxide separation tower, said rare ammonia carbon aqueous solution is sent into from the middle part and/or the bottom of said carbon dioxide separation tower from the isolated rare ammonia carbon aqueous solution of the side line of said water separation column.In traditional ammonia carbon separation method, the required water of carbon knockout tower is all from the bottom of the separated form water Tata.The utility model has only the purity that adds carbon knockout tower top than the bottom of higher water from water separation column; So that make carbon separate the ammonia content≤50pm of the carbon dioxide that cat head steams; And send in the carbon knockout tower, the water of bottom, then be that the ammonia from the extraction of water separation column side line contains a spot of rare ammonia carbon aqueous solution.Because this part water is about 70% ~ 90% of the water that adds the carbon knockout tower, changes by after the extraction of water separation column side line, the load of water separation column alleviates greatly, energy consumption significantly reduces.
(7) the described piece-rate system that is used for ammonia and carbon dioxide gas mixture of the utility model; Recirculation cooler of extraction liquid cooler, ammonia knockout tower etc. at the bottom of the reflux condenser of water separation column, the separated form water Tata; All adopt aerial cooler; In traditional ammonia carbon separation method, when hot fluid need cool off, generally all adopting with the recirculated cooling water was the cooler of cooling medium.In the described method of the utility model, the consumption of recirculated cooling water is significantly reduced.
Description of drawings
In order to make the described technical scheme of the utility model be convenient to more understand, the described technical scheme of the utility model is done further elaboration below in conjunction with the accompanying drawing and the specific embodiment.
Shown in Figure 1 is the isobaric phasor of ammonia, carbon dioxide, water ternary system;
Shown in Figure 2 is the described sketch map that is used for the piece-rate system of ammonia and carbon dioxide gas mixture of the utility model;
Shown in Figure 3 is the sketch map of the described ammonia knockout tower of the utility model operating pressure ammonia and carbon dioxide gas mixture piece-rate system when being 18bar;
Shown in Figure 4 is the separation process scheme figure of ammonia and carbon dioxide gas mixture in the prior art.
Wherein, Reference numeral is:
One section on 1-compressor; Two sections on 2-compressor; 3-carbon dioxide separation tower; 4,9-reboiler; The 5-water separation column; 6-side line extraction pump; 7,8, the 10-heat exchanger; 11, the 26-reflux condenser; The 12-cooler; 13, the 24-recirculation cooler; 14, the 25-circulating pump; 15,17,27-booster; 16-ammonia knockout tower; One section of 18-helical-lobe compressor; 19, the 21-segregator; Two sections of 20-helical-lobe compressors; The 22-ammonia condenser; The lazy tower of washing of 23-.
The specific embodiment
Embodiment 1
The piece-rate system that is used for ammonia and carbon dioxide gas mixture described in the present embodiment is as shown in Figure 2, comprising:
Carbon dioxide separation tower 3, the bottom of said carbon dioxide separation tower 3 be with reboiler 4, is connected with heat exchanger 8 and heat exchanger 7 with ammonia carbon aqueous solution outlet at the bottom of said carbon dioxide separation tower 3 towers;
Be connected with water separation column 5 with said carbon dioxide separation tower 3; Water separation column 5 bottoms are with reboiler 9; The top is provided with reflux condenser 11; Said reflux condenser 11 is an air cooler, and the middle part of said water separation column 5 is provided with side line extraction pump 6, and said side line extraction pump 6 is from the rare ammonia carbon of the side line extraction aqueous solution of said water separation column 5; Be connected with booster 17, heat exchanger 10 and cooler 12 with the bottom delivery port of said water separation column 5, said cooler 12 is an air cooler;
Be connected with ammonia knockout tower 16 with said separated form water 5 towers, said ammonia knockout tower 16 tops are with reflux condenser 26, and the middle part is with circulating pump 14 and recirculation cooler 13, and said recirculation cooler 13 is an air cooler; Dense ammonia carbon aqueous solution outlet at the bottom of the said ammonia knockout tower is connected with booster 15, heat exchanger 10, heat exchanger 7.
Said system also is provided with the gas compressing apparatus that said ammonia and carbon dioxide gas mixture are compressed, and the outlet of said gas compressing apparatus is connected with said carbon dioxide separation tower 3.Gas compressing apparatus described in the present embodiment is the multistage gas compressing apparatus, comprises two section 2 on a section 1 on compressor and compressor.
Separation method based on the piece-rate system described in the present embodiment is:
A. be that the melamine tail gas of 4bar is sent into tail-gas compressor and compressed for one section 1 with pressure; One section outlet pressure is 8.6bar; Temperature rises to 236 ℃; Spray into by temperature behind rare ammonia carbon aqueous solution of water separation column 5 side line extraction and reduce to 140 ℃, and then send into two section 2 on compressor and continue compression, gas is compressed to 18bar, 234 ℃.
B. the gas after will compressing is sent into carbon dioxide separation tower 3 bottoms, and the upper, middle and lower portion of carbon dioxide separation tower 3 sends into respectively from the water at the bottom of water separation column 5 towers, from rare ammonia carbon aqueous solution of water separation column 5 side line extraction with from the mixed liquor of the dense ammonia carbon aqueous solution of ammonia knockout tower 16 bottoms; Anticorrosion air gets into carbon dioxide separation tower 3 through reboiler 4.The operating pressure of carbon dioxide separation tower 3 is 18bar, 70 ~ 90 ℃ of tower top temperatures, 165 ~ 170 ℃ of tower still temperature; The carbon dioxide of ammonia content≤50ppm is discharged from the cat head of carbon dioxide separation tower 3, and the ammonia carbon aqueous solution that contains amounts of carbon dioxide is discharged at the bottom of tower.
The ammonia carbon aqueous solution that contains amounts of carbon dioxide of c. discharging at the bottom of carbon dioxide separation tower 3 towers is sent into water separation column 5 behind heat exchanger 8 and heat exchanger 7.Anticorrosion air gets into water separation column 5 through reboiler 9.The operating pressure of water separation column 5 is about 2bar, 68 ~ 74 ℃ of reflux condenser 11 outlet temperatures, 117 ~ 121 ℃ of tower still temperature.Rare ammonia carbon aqueous solution of water separation column side line extraction pump extraction is sent to the outlet of a section 1 of carbon dioxide separation tower 3 and tail-gas compressor respectively; The water of bottom extraction boosts, is sent to carbon dioxide separation tower 3 tops and lazy tower 23 tops of washing respectively after 12 coolings of heat exchanger 10 and cooler through booster 17; Said cooler 12 is an air cooler, and the mist of ammonia, carbon dioxide and water steams from the top of water separation column.
D. the mist of the ammonia, carbon dioxide and the water that steam of water separation column 5 tops is sent to ammonia knockout tower 16 bottoms, sends into the ammoniacal liquor of circulation from ammonia knockout tower 16 tops.The operating pressure of ammonia knockout tower 16 is 2bar, 48 ~ 53 ℃ of reflux condenser 26 outlet temperatures, 60 ~ 71 ℃ of tower still temperature.The dense ammonia carbon aqueous solution of ammonia knockout tower 16 bottom extraction is sent into carbon dioxide separation tower 3 behind booster 15, heat exchanger 10, heat exchanger 7, isolate ammonia from the top of said ammonia knockout tower 16.
Embodiment 2
The piece-rate system that is used for ammonia and carbon dioxide gas mixture described in the present embodiment is with embodiment 1, based on the separation method of the piece-rate system described in the present embodiment is:
A. be that the melamine tail gas of 4bar is sent into tail-gas compressor and compressed for one section 1 with pressure, one section outlet pressure is 8.5bar, and temperature rises to 234 ℃, sprays into by temperature behind rare ammonia carbon aqueous solution of water separation column 5 side line extraction and reduces to 140 ℃.And then send into two section 2 on compressor and continue compression, gas is compressed to 15bar, 223 ℃.
B. the gas after will compressing is sent into carbon dioxide separation tower 3 bottoms, and the upper, middle and lower portion of carbon dioxide separation tower 3 sends into respectively from the water at the bottom of water separation column 5 towers, from rare ammonia carbon aqueous solution of water separation column 5 side line extraction with from the mixed liquor of the dense ammonia carbon aqueous solution of ammonia knockout tower 16 bottoms.Anticorrosion air gets into carbon dioxide separation tower 3 through reboiler 4.The operating pressure of carbon dioxide separation tower 3 is 15bar, 70 ~ 80 ℃ of tower top temperatures, 155 ~ 161 ℃ of tower still temperature.The carbon dioxide of ammonia content≤50ppm is discharged from carbon dioxide separation tower 3 cats head; The ammonia carbon aqueous solution that contains amounts of carbon dioxide is discharged at the bottom of tower.
The ammonia carbon aqueous solution that contains amounts of carbon dioxide of c. discharging at the bottom of carbon dioxide separation tower 3 towers is sent into water separation column 5 behind heat exchanger 8 and heat exchanger 7.Water separation column 5 bottoms are with reboiler 9, and anticorrosion air gets into water separation column through reboiler 9.The operating pressure of water separation column 5 is about 2bar, 68 ~ 74 ℃ of reflux condenser 11 outlet temperatures, 117 ~ 121 ℃ of tower still temperature.Rare ammonia carbon aqueous solution of water separation column 5 side line extraction is sent to carbon dioxide separation tower 3 and one section 1 outlet of tail-gas compressor respectively; The water of bottom extraction boosts, is sent to carbon dioxide separation tower 3 tops and lazy tower 23 tops of washing respectively after 12 coolings of heat exchanger 10 and cooler through booster 17; Said cooler 12 is an air cooler, and the mist of ammonia, carbon dioxide and water steams from the top of water separation column 5.
D. the mist of the ammonia, carbon dioxide and the water that steam of water separation column 5 tops is sent to ammonia knockout tower 16 bottoms, sends into the ammoniacal liquor of circulation from ammonia knockout tower 16 tops.The operating pressure of ammonia knockout tower 16 is 2bar, 48 ~ 53 ℃ of reflux condenser 26 outlet temperatures, 60 ~ 71 ℃ of tower still temperature.The dense ammonia carbon aqueous solution of ammonia knockout tower 16 bottom extraction is sent into carbon dioxide separation tower 3 behind booster 15, heat exchanger 10, heat exchanger 7, isolate ammonia from the top of said ammonia knockout tower 16.
Embodiment 3
The piece-rate system that is used for ammonia and carbon dioxide gas mixture described in the present embodiment is with embodiment 1, based on the separation method of the piece-rate system described in the present embodiment is:
A. be that the melamine tail gas of 4bar is sent into tail-gas compressor and compressed for one section 1 with pressure, one section outlet pressure is 10.1bar, and temperature rises to 257 ℃, sprays into by temperature behind rare ammonia carbon aqueous solution of water separation column 5 side line extraction and reduces to 140 ℃.And then send into two section 2 on compressor and continue compression, gas is compressed to 25bar, 258 ℃.
B. the gas after will compressing is sent into carbon dioxide separation tower 3 bottoms, and the upper, middle and lower portion of carbon dioxide separation tower 3 sends into respectively from the water at the bottom of water separation column 5 towers, from rare ammonia carbon aqueous solution of water separation column 5 side line extraction with from the mixed liquor of the dense ammonia carbon aqueous solution of ammonia knockout tower 16 bottoms.Anticorrosion air gets into carbon dioxide separation tower 3 through reboiler 4.The operating pressure of carbon dioxide separation tower 3 is 25bar, 80 ~ 90 ℃ of tower top temperatures, 180 ~ 186 ℃ of tower still temperature.The carbon dioxide of ammonia content≤50ppm is discharged from carbon dioxide separation tower 3 cats head; The ammonia carbon aqueous solution that contains amounts of carbon dioxide is discharged at the bottom of tower.
The ammonia carbon aqueous solution that contains amounts of carbon dioxide of c. discharging at the bottom of carbon dioxide separation tower 3 towers is sent into water separation column 5 behind heat exchanger 8 and heat exchanger 7.Anticorrosion air gets into water separation column 5 through reboiler 9.The operating pressure of water separation column 5 is about 2bar, 68 ~ 74 ℃ of reflux condenser 11 outlet temperatures, 117 ~ 121 ℃ of tower still temperature.Rare ammonia carbon aqueous solution of water separation column 5 side line extraction is sent to carbon dioxide separation tower 3 and one section 1 outlet of tail-gas compressor respectively; The water of bottom extraction boosts, is sent to carbon dioxide separation tower 3 tops and lazy tower 23 tops of washing respectively after 12 coolings of heat exchanger 10 and cooler through booster 17; Said cooler 12 is an air cooler, and the mist of ammonia, carbon dioxide and water steams from the top of water separation column 5.
D. the mist of the ammonia, carbon dioxide and the water that steam of water separation column 5 tops is sent to ammonia knockout tower 16 bottoms, sends into the ammoniacal liquor of circulation from ammonia knockout tower 16 tops.The operating pressure of ammonia knockout tower 16 is 2bar, 48 ~ 53 ℃ of reflux condenser 26 outlet temperatures, 60 ~ 71 ℃ of tower still temperature.The dense ammonia carbon aqueous solution of ammonia knockout tower 16 bottom extraction is sent into carbon dioxide separation tower 3 behind booster 15, heat exchanger 10, heat exchanger 7, isolate ammonia from the top of said ammonia knockout tower 16.
Embodiment 4
The piece-rate system that is used for ammonia and carbon dioxide gas mixture described in the present embodiment is with embodiment 1, based on the separation method of the piece-rate system described in the present embodiment is:
A. be that the melamine tail gas of 4bar is sent into tail-gas compressor and compressed for one section 1 with pressure, one section outlet pressure is 8.6bar, and temperature rises to 234 ℃, sprays into by temperature behind rare ammonia carbon aqueous solution of water separation column 5 side line extraction and reduces to 140 ℃.And then send into two section 2 on compressor and continue compression, gas is compressed to 18bar, 234 ℃.
B. the gas after will compressing is sent into carbon dioxide separation tower 3 bottoms, and the upper, middle and lower portion of carbon dioxide separation tower 3 sends into respectively from the water at the bottom of water separation column 5 towers, from rare ammonia carbon aqueous solution of water separation column 5 side line extraction with from the mixed liquor of the dense ammonia carbon aqueous solution of ammonia knockout tower 16 bottoms.Anticorrosion air gets into carbon dioxide separation tower 3 through reboiler 4.The operating pressure of carbon dioxide separation tower 3 is 18bar, 70 ~ 90 ℃ of tower top temperatures, 165 ~ 170 ℃ of tower still temperature.The carbon dioxide of ammonia content≤50ppm is discharged from carbon dioxide separation tower 3 cats head; The ammonia carbon aqueous solution that contains amounts of carbon dioxide is discharged at the bottom of tower.
The ammonia carbon aqueous solution that contains amounts of carbon dioxide of c. discharging at the bottom of carbon dioxide separation tower 3 towers is sent into water separation column 5 behind heat exchanger 8 and heat exchanger 7.Anticorrosion air gets into water separation column 5 through reboiler 9.The operating pressure of water separation column 5 is about 4bar, 85 ~ 95 ℃ of reflux condenser 11 outlet temperatures, 138 ~ 143.5 ℃ of tower still temperature.Rare ammonia carbon aqueous solution of water separation column 5 side line extraction is sent to carbon dioxide separation tower 3 and one section 1 outlet of tail-gas compressor respectively; The water of bottom extraction boosts, is sent to carbon knockout tower top and lazy tower 23 tops of washing respectively after 12 coolings of heat exchanger 10 and cooler through booster 17, and said cooler 12 is an air cooler, and the mist of ammonia, carbon dioxide and water steams from the top of water separation column 5.
D. the mist of the ammonia, carbon dioxide and the water that steam of water separation column 5 tops is sent to ammonia knockout tower 16 bottoms, sends into the ammoniacal liquor of circulation from ammonia knockout tower 16 tops.The operating pressure of ammonia knockout tower 16 is 4bar, 55 ~ 62 ℃ of reflux condenser 26 outlet temperatures, 75 ~ 85 ℃ of tower still temperature.The dense ammonia carbon aqueous solution of ammonia knockout tower 16 bottom extraction is sent into carbon dioxide separation tower 3 behind booster 15, heat exchanger 10, heat exchanger 7, isolate ammonia from the top of said ammonia knockout tower 16.
Embodiment 5
The piece-rate system of ammonia described in the present embodiment and carbon dioxide gas mixture is as shown in Figure 3, comprising:
Carbon dioxide separation tower 3, the bottom of said carbon dioxide separation tower 3 be with reboiler 4, is connected with booster 27, heat exchanger 8 and heat exchanger 7 with ammonia carbon aqueous solution outlet at the bottom of said carbon dioxide separation tower 3 towers;
Be connected with water separation column 5 with said carbon dioxide separation tower 3; Water separation column 5 bottoms are with reboiler 9; The top is provided with reflux condenser 11; Said reflux condenser 11 is an air cooler, and the middle part of said water separation column 5 is provided with side line extraction pump 6, and said side line extraction pump 6 is from the rare ammonia carbon of the side line extraction aqueous solution of said water separation column 5; Be connected with booster 17 with the bottom delivery port of said water separation column 5;
Be connected with ammonia knockout tower 16 with said separated form water 5 towers, said ammonia knockout tower 16 tops are with reflux condenser 26, and the middle part is with circulating pump 14 and recirculation cooler 13, and said recirculation cooler 13 is an air cooler; Dense ammonia carbon aqueous solution outlet at the bottom of the said ammonia knockout tower is connected with booster 15.
Said system also is provided with the gas compressing apparatus that said ammonia and carbon dioxide gas mixture are compressed, and the outlet of said gas compressing apparatus is connected with said carbon dioxide separation tower 3.Gas compressing apparatus described in the present embodiment is the multistage gas compressing apparatus, comprises two section 2 on a section 1 on compressor and compressor.
In the separation method based on the piece-rate system described in the present embodiment, the operating pressure of carbon knockout tower, water separation column, ammonia knockout tower is 18bar, and the ammonia that the ammonia knockout tower is told is that the ammonia condenser of cooling medium is condensed into liquefied ammonia in order to water.Concrete grammar is following:
A. be that the melamine tail gas of 4bar is sent into tail-gas compressor and compressed for one section 1 with pressure, one section outlet pressure is 8.6bar, and temperature rises to 234 ℃, sprays into by temperature behind rare ammonia carbon aqueous solution of water separation column 5 side line extraction and reduces to 140 ℃.And then send into two section 2 on compressor and continue compression, gas is compressed to 18bar, 234 ℃.
B. the gas after will compressing is sent into carbon dioxide separation tower 3 bottoms, and the upper, middle and lower portion of carbon dioxide separation tower 3 sends into respectively from the water at the bottom of water separation column 5 towers, from rare ammonia carbon aqueous solution of water separation column 5 side line extraction with from the mixed liquor of the dense ammonia carbon aqueous solution of ammonia knockout tower 16 bottoms.Carbon dioxide separation tower 3 bottoms are with reboiler 4, and anticorrosion air gets into carbon dioxide separation tower 3 through reboiler 4.The operating pressure of carbon dioxide separation tower 3 is 18bar, 70 ~ 90 ℃ of tower top temperatures, 165 ~ 170 ℃ of tower still temperature.The carbon dioxide of ammonia content≤50ppm is discharged from carbon dioxide separation tower 3 cats head; The ammonia carbon aqueous solution that contains amounts of carbon dioxide is discharged at the bottom of tower.
The ammonia carbon aqueous solution that contains amounts of carbon dioxide of c. discharging at the bottom of carbon dioxide separation tower 3 towers is pumped by pump 27, behind heat exchanger 8 and heat exchanger 7, sends into water separation column 5.Water separation column 5 bottoms are with reboiler 9, and anticorrosion air gets into water separation column 5 through reboiler 9.The top of water separation column 5 is provided with reflux condenser 11, and said reflux condenser 11 is an air cooler, and the middle part of water separation column 5 is provided with side line extraction pump 6.The operating pressure of water separation column 5 is about 18bar, 137 ~ 142 ℃ of reflux condenser 11 outlet temperatures, 200 ~ 206 ℃ of tower still temperature.Rare ammonia carbon aqueous solution of water separation column 5 side line extraction is sent to carbon dioxide separation tower 3 and one section 1 outlet of tail-gas compressor respectively; The water of bottom extraction is sent to carbon knockout tower 3 tops and lazy tower 23 tops of washing respectively after pump 17, heat exchanger 7 and cooler 12 coolings, said cooler 12 is an air cooler, and the mist of ammonia, carbon dioxide and water steams from the top of water separation column 5.
D. the mist of the ammonia, carbon dioxide and the water that steam of water separation column 5 tops is sent to ammonia knockout tower 16 bottoms.Send into the ammoniacal liquor of circulation from ammonia knockout tower 16 tops, ammonia knockout tower 16 tops are with reflux condenser 26, and the middle part is with circulating pump 14 and recirculation cooler 13, and said recirculation cooler 13 is an air cooler.The operating pressure of ammonia knockout tower 16 is 18bar, 42 ~ 45 ℃ of reflux condenser 26 outlet temperatures, 97 ~ 140 ℃ of tower still temperature.The dense ammonia carbon aqueous solution of ammonia knockout tower 16 bottom extraction is sent into carbon dioxide separation tower 3 through pump 15, isolates ammonia from the top of said ammonia knockout tower 16.
E. the isolated ammonia in the top of ammonia knockout tower 16 gets into ammonia condenser 22, and ammonia is condensed into liquefied ammonia, and the inert gas that is not condensed is sent to the lazy tower 23 of washing.The lazy tower 23 of washing is with circulating pump 25 and recirculation cooler 24, and the water of supplementing water and circulation is sent into the lazy top of washing tower 23.The inert gas of ammonia content≤30ppm after the washing enters atmosphere by cat head, and the ammoniacal liquor at the bottom of the tower is sent to ammonia knockout tower 16.
The compression of ammonia
The isolated ammonia in ammonia knockout tower 16 tops among the embodiment 1-4 is sent to helical-lobe compressor to be compressed for one section 18; Ammonia after the compression gets into segregator 19 and is chilled to 44 ~ 46 ℃; The liquid part that condensation is got off is sent to and sprays into one section inlet tube, and remaining liquid is sent to ammonia knockout tower 16.Gas that segregator 19 comes out gets into two sections of helical-lobe compressors and continues to be compressed to and get into segregator 21 behind the 18bar and be chilled to 45 ~ 47 ℃, and the liquid part that condensation is got off is sent to and sprays into the inlet tube of two section 20 of helical-lobe compressor, and remaining liquid is sent to ammonia knockout tower 16.The gas that is come out by segregator 21 gets into ammonia condenser 22, and ammonia is condensed into liquefied ammonia, and the inert gas that is not condensed is sent to the lazy tower 23 of washing.The lazy tower 23 of washing is with circulating pump 25 and recirculation cooler 24, and the water of supplementing water and circulation is sent into the lazy top of washing tower 23.The inert gas of ammonia content≤30ppm after the washing enters atmosphere by cat head, and the ammoniacal liquor at the bottom of the tower is sent to the ammonia knockout tower.
All adopted the mode of two sections compressions that melamine tail gas is compressed in the foregoing description,, also can adopt single hop or the mode more than two sections to compress as selectable embodiment.In addition; As preferred embodiment, in order further to cut down the consumption of energy, the reflux condenser 11 in the foregoing description, cooler 12, recirculation cooler 13 are air cooler; As selectable embodiment, said apparatus also can adopt the cooler of other form; Same as preferred embodiment, the middle part of the water separation column 5 in the foregoing description is provided with side line extraction pump 6, as selectable embodiment, also can not adopt rare ammonia carbon aqueous solution of said water separation column 5 side line extraction.
Need to prove that also the separation method described in the present invention is not only applicable to melamine tail gas, be applicable to that also ammonia and carbon dioxide mass ratio are the separating of mist of ammonia, carbon dioxide and the water of arbitrary ratio and water content≤15% between the 0.5-1.5.
The energy-saving effect test of embodiment and comparative example
In order to prove the energy-saving effect of the said technical scheme of the utility model, quantity of steam, electric weight and the cooling water inflow of one ton of liquefied ammonia consumption of every recovery in embodiment and the comparative example are measured at present, be listed in the table below:
Table 1: the energy consumption of 1 ton of liquefied ammonia of every recovery
Obviously, the foregoing description only be for explanation clearly done for example, and be not qualification to embodiment.For the those of ordinary skill in affiliated field, on the basis of above-mentioned explanation, can also make other multi-form variation or change.Here need not also can't give all embodiments exhaustive, and conspicuous variation of being extended out thus or change still are among the protection domain that the utility model creates.
Claims (6)
1. piece-rate system that is used for ammonia and carbon dioxide gas mixture comprises:
The carbon dioxide separation tower;
Be connected with water separation column with said carbon dioxide separation tower;
Be connected with the ammonia knockout tower with said water separation column;
It is characterized in that,
Said system also is provided with the gas compressing apparatus that said ammonia and carbon dioxide gas mixture are compressed, and the outlet of said gas compressing apparatus is connected with said carbon dioxide separation tower.
2. system according to claim 1 is characterized in that, said gas compressing apparatus is the multistage gas compressing apparatus.
3. the piece-rate system of ammonia according to claim 1 and 2 and carbon dioxide gas mixture is characterized in that the top of said water separation column is provided with reflux condenser, and said reflux condenser is an air cooler.
4. system according to claim 3 is characterized in that the bottom of said ammonia knockout tower and/or middle part are provided with circulating pump and recirculation cooler.
5. system according to claim 4 is characterized in that the recirculation cooler of said ammonia knockout tower is an air cooler.
6. according to claim 4 or 5 described systems, it is characterized in that the middle part of said water separation column is provided with side line extraction pump.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2012202778517U CN202620989U (en) | 2012-06-13 | 2012-06-13 | Separation system for mixed gas of ammonia and carbon dioxide |
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| Application Number | Priority Date | Filing Date | Title |
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| CN2012202778517U CN202620989U (en) | 2012-06-13 | 2012-06-13 | Separation system for mixed gas of ammonia and carbon dioxide |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102671515A (en) * | 2012-06-13 | 2012-09-19 | 北京烨晶科技有限公司 | System for separating ammonia and carbon dioxide mixed gas |
| CN103111159A (en) * | 2013-02-26 | 2013-05-22 | 北京烨晶科技有限公司 | Melamine tail gas treatment method |
| CN103301722A (en) * | 2013-06-06 | 2013-09-18 | 四川亚连科技有限责任公司 | Nitrogen-reduction denitration ammonia water device and method for preparing ammonium carbonate or ammonium bicarbonate as well as use thereof |
-
2012
- 2012-06-13 CN CN2012202778517U patent/CN202620989U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102671515A (en) * | 2012-06-13 | 2012-09-19 | 北京烨晶科技有限公司 | System for separating ammonia and carbon dioxide mixed gas |
| CN103111159A (en) * | 2013-02-26 | 2013-05-22 | 北京烨晶科技有限公司 | Melamine tail gas treatment method |
| CN103301722A (en) * | 2013-06-06 | 2013-09-18 | 四川亚连科技有限责任公司 | Nitrogen-reduction denitration ammonia water device and method for preparing ammonium carbonate or ammonium bicarbonate as well as use thereof |
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Owner name: SICHUAN GOLDEN-ELEPHANT SINCERITY CHEMICAL CO., LT Free format text: FORMER OWNER: SICHUAN GOLDEN-ELEPHANT SINCERITY CHEMICAL CO., LTD. Effective date: 20131106 |
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Effective date of registration: 20131106 Address after: 100084, room 605, building C, Tsinghua Science and Technology Park, No. 1, Zhongguancun East Road, Haidian District, Beijing Patentee after: Beijing Edgein Technology Co., Ltd. Patentee after: Sichuan Golden-Elephant Sincerity Chemical Co., Ltd. Patentee after: JIANGSU JINXIANG SAIRUI CHEMICAL SCIENCE & TECHNOLOGY CO., LTD. Address before: 100084, room 605, building C, Tsinghua Science and Technology Park, No. 1, Zhongguancun East Road, Haidian District, Beijing Patentee before: Beijing Edgein Technology Co., Ltd. Patentee before: Sichuan Golden-Elephant Sincerity Chemical Co., Ltd. |
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