CN102276544A - Production equipment, energy-saving production system and production method for melamine - Google Patents
Production equipment, energy-saving production system and production method for melamine Download PDFInfo
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- CN102276544A CN102276544A CN201110176102A CN201110176102A CN102276544A CN 102276544 A CN102276544 A CN 102276544A CN 201110176102 A CN201110176102 A CN 201110176102A CN 201110176102 A CN201110176102 A CN 201110176102A CN 102276544 A CN102276544 A CN 102276544A
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Abstract
The invention discloses a heat-conducting oil hollow blade cooling crystallizer for melamine, an energy-saving production system consisting of the crystallizer and a method for producing the melamine by using the system. The invention is characterized in that: a hot air cooling crystallization system consisting of the heat-conducting oil hollow blade cooling crystallizer, a hot air purification device, a heat-conducting oil steam generator and a cyclone separator is adopted. In the invention, the heat-conducting oil hollow blade cooling crystallizer which is provided with a movable heat exchange surface and has the heat exchange surface with a self-cleaning function is used for crystallizing and recovering the melamine for the first time; heat-conducting oil is adopted as a melamine crystallization cooling medium for the first time; heat is transferred to soft water to produce steam by the heat-conducting oil; the heat-conducting oil is in a closed cycle without heat loss; and thus, high-efficiency recycling of waste heat of cooling crystallization is realized, energy is saved and consumption is reduced.
Description
Technical field
The present invention relates to chemical field, relate in particular to Production of Cyanuramide system and production technique.
Background technology
At present, domestic Production of Cyanuramide technology mainly contains traditional normal pressure one-step method, low pressure single stage method and normal pressure two-step approach; Other has the high pressure single stage method of few part.Here the normal pressure of saying is meant that system pressure is 0～0.2MPa, and low pressure is meant that system pressure is 0.2～1MPa, and high pressure is meant that system pressure is greater than 1MPa.Relevant with the present invention is traditional normal pressure one-step method, low pressure single stage method and normal pressure two-step approach.(traditional normal pressure one-step method and low pressure one-step method production process system are identical, and difference is the system pressure difference)
Tradition is normal, low pressure single stage method preparation technology of melamine system as shown in Figure 1, mainly form by Salt heater, fluidized-bed reactor, hot gas water cooler, hot gas filtration device, hot gas crystallisation by cooling system, compressor and tail gas absorption system etc.
Tradition normal pressure two-step approach preparation technology of melamine system as shown in Figure 2, and is main by rough systems such as the Salt heater of producing crude product, fluidized-bed reactor, hot gas filtration device, hot gas crystallisation by cooling system, water wash column 1-4, ammonia cool-drying device, carrier gas compressor, refrigerant condensers; And refining systems such as the dissolving vessel that produces choice goods, well heater, strainer, water cooler, crystallizer, separator, baker, pulverizer are formed.
Wherein, hot gas crystallisation by cooling system normal, the low pressure single stage method mainly is made up of parts such as steam system, crystallizer, cyclonic separator, circulating cold air blower fan, liquid urine recycle pump, liquid urine washing tower, gas-liquid separator and liquid urine water coolers.
Often, the Production Flow Chart technology of low pressure single stage method is: about 380 degrees centigrade the high temperature hybrid technique gas (trimeric cyanamide, ammonia, carbonic acid gas) that fluidized-bed reactor comes out cools to (high boiling point by-products produced crystallizing out) about 320 degrees centigrade through the hot gas water cooler, enters the hot gas filtration device again and filters; Warm hybrid technique gas enters crystallizer downwards by the crystallizer top pure after the hot gas filtration device filters; About 140 degrees centigrade the cold process gas of coming from air collector upwards enters crystallizer through six to eight ring-like jet pipes of crystallizer middle and lower part, and the trimeric cyanamide crystallization that crosses in the process of hot and cold process gas is separated out; Cool to low-temperature mixed process gas (ammonia, carbonic acid gas) about 210 degrees centigrade and mix and to carry melamine crystals secretly and enter cyclonic separator through the crystallizer outlet at bottom, isolated melamine crystals enters finished product bin by the cyclonic separator outlet at bottom; The ammonia that comes out from the cyclonic separator top and the hybrid technique gas of carbonic acid gas enter liquid urine washing tower downwards by the top after through the circulating cold air blower fan, downward with the liquid urine mixing following current about 130 degree of urinating liquid urine nozzle ejection in the washing tower from liquid, through cooling to the cold process gas about 140 degrees centigrade behind the mixing traverse baffle in the tower, cold process gas enters respectively in two to eight groups of gas-liquid separators through liquid urine washing tower bottom outlet together with liquid urine, and the liquid urine that is warmed up to about 136 degrees centigrade is imported in the liquid urine storage tank by the separator bottom; Liquid urine enters liquid urine water cooler cooling (heat is dispersed in the atmosphere by air-cooler by cooling circulating water) by liquid urine recycle pump, enters in the liquid urine washing tower after being cooled to about 130 degrees centigrade again and continues circulation; Cool to enter after cold process gas about 140 degrees centigrade is come out by two to eight groups of gas-liquid separator tops and be divided into three tunnel: one tunnel (major part) device that decrystallizes in the air collector and continue the circulation cooling; The second tunnel (seldom part) aspiration that truncates is received; Go fluidized-bed reactor to continue circulation behind the Third Road process compressor pressure-raising.
Wherein, the hot gas crystallisation by cooling system of normal pressure two-step approach mainly is made up of five placed in-line traps.
The Production Flow Chart technology of above-mentioned two-step approach is: about 380 degrees centigrade the high temperature hybrid technique gas (trimeric cyanamide that fluidized-bed reactor comes out, ammonia, carbonic acid gas) entering the hot gas filtration device filters, the high boiling point by-products produced high temperature hybrid technique gas that contains after the filtration of hot gas filtration device enters in five placed in-line traps successively, the temperature of high temperature hybrid technique is cooled to about 140 degrees centigrade to outside naturally radiating and cooling from about the 380 degrees centigrade outside wall surface by five traps, trimeric cyanamide obtains along with being reduced in spontaneous nucleation sedimentation in five traps of temperature together with by product, device parking (about 5～6 days) is regularly opened five traps bottom blind plates and is adopted manual type to carry out discharging, can only batch production, gained trimeric cyanamide product is because of containing impurity such as by product, off qualityly can only calculate crude product, crude product also needs again through dissolving, heating, filter, cooling, crystallization, separate, oven dry, refining systems such as pulverizing just can obtain the trimeric cyanamide salable product, both finished product; The low temperature process gas that is reduced to about 140 degrees centigrade through temperature behind five trap crystallisation by cooling is reduced to subzero about 6 degrees centigrade through temperature behind four placed in-line water wash columns and the ammonia cool-drying device again, and ammonia cool-drying device is furnished with refrigerant condenser and carries out the ammonia circulation; Go fluidized-bed reactor to continue circulation behind subzero about the 6 degrees centigrade refrigerating process gas process compressor pressure-raising.
The common deficiency of the hot gas crystallisation by cooling system of above-mentioned traditional technology is: system architecture complexity, the waste heat in the crystallisation by cooling process all do not have to recycle, and waste heat is dispersed in the atmosphere, causes the significant wastage of heat, and system energy consumption is very high.
Often, the low pressure single stage method also has following not enough:
1, equipment such as crystallizer, liquid urine recycle pump, liquid urine washing tower, gas-liquid separator and liquid urine water cooler and pipeline valve etc. are stainless steel, major part is expensive 316L stainless steel, and equipment huge numerous, pipeline is numerous and diverse, it is big to take the production space, and equipment and supporting construction investment are huge;
2, crystallization is six to seven times of normal reaction circulation technology tolerance with the circulation air conditioning quantity, and the cold air blower fan that required power is very big carries out circulating cold air; Liquid urine internal circulating load is also very big, also needs powerful liquid urine recycle pump to finish, and they all need to consume a large amount of electric power, and energy consumption is very high;
3, crystallisation by cooling system process equipment complexity is numerous, and Production Flow Chart is long, complicated operation, and the control difficulty is big;
4, liquid urine not only can cause a large amount of power consumptions in continuous heating-cooling pump circulation process, also can occur the high temperature urea decomposition along with technological fluctuation and produce part biuret phenomenon, has increased the consumption of urea;
5, liquid urine easily crystallization at low temperatures, all devices that contacts with liquid urine and pipeline all need steam system companion heat; Crystallizer also needs steam system companion heat in addition, and it is a lot of that energy consumption is increased;
6, always carry the debris urine of small part in the process gas behind the gas-liquid separator secretly, both increased the consumption of urea, can make pipeline and equipment knot wall again, influence the production cycle;
The normal pressure two step method also has following not enough:
1, device needs regularly to stop and opens trap bottom blind plate and adopt manual type to carry out discharging, can only batch production, and can't continuous production;
2, trap gained trimeric cyanamide product is because of containing impurity such as by product, quality does not reach the finished product index, can only calculate crude product, crude product also needs just to obtain the trimeric cyanamide finished product through numerous and diverse refining systems such as dissolving, heating, filtration, cooling, crystallization, separation, oven dry, pulverizing again, can only two-step approach production;
3, Production Flow Chart is long, energy consumption is high, pollution is big;
4, trap crystallisation by cooling effect is subjected to the influence of trap knot wall, ambient temperature and controlling level bigger, and temperature was than difficult control before 1# washed tower.Particularly in summer, because of in ambient temperature height, the trap during high charge level the required useful space of crystallisation by cooling reduce, temperature can be higher than usual before 1# washed tower, and circulation gas very easily is with material to enter 1# and is washed in the tower ammoniacal liquor, causes the unnecessary material loss and the rising of consumption;
5, stopping before each discharging expect to activate and drive after system's temperature-rise period all need more than ten hour time, big energy consumption equipment such as molten salt furnace, compressor, refrigerator all is in the running light around here, has promptly increased coal consumption, power consumption, has influenced output again;
6, each discharging process all needs 6-8 hour time, has many triamine dust and surplus ammonia can fly away in the air during artificial blowing, promptly forms environmental pollution and causes very big material waste again;
7, because trap knot wall problem needs manually the trap outer wall to be carried out timing beats, labour intensity is big, also produces very big noise pollution;
Summary of the invention
The above-mentioned deficiency of conventional process techniques such as, low pressure single stage method existing normal and normal pressure two-step approach for overcoming, the hot gas crystallisation by cooling system that the present invention is directed to traditional technologys such as normal, low pressure single stage method and normal pressure two-step approach carries out energy saving optimizing and comprehensively improves the energy-conservation production system of inventing out a kind of trimeric cyanamide thermal oil hollow blade crystallisation by cooling machine and being made up of this crystallisation by cooling machine.
The present invention provides a kind of usefulness processing method that this system produces trimeric cyanamide simultaneously.
Thermal oil hollow blade crystallisation by cooling machine structure of the present invention is, it comprises a chuck shape cylindrical shell, and an end top of cylindrical shell is provided with and is provided with the mixture outlet that links to each other with cyclonic separator bottom the combi inlet port that links to each other with the outlet of hot gas purification device, the other end; Two to four tubular shafts are installed on the axis plane in cylindrical shell; All be furnished with the fan-shaped blade of hollow on every tubular shaft at interval, the fan-shaped blade positioned opposite or the staggered arrangement of two adjacent vacant axles; The cavity of fan-shaped blade communicates with the cavity of tubular shaft; Be fixed with spaced apart scraper plate on cylinder inboard wall, scraper plate stretches between the fan-shaped blade, guarantees that all fan-shaped blade both sides all are furnished with scraper plate, and the mutual gap of scraper plate and fan-shaped blade is the 6-10 millimeter; Tubular shaft rotates with the lower velocity that per minute 3 to 18 changes by transmission mechanism, and the turning direction of two adjacent vacant axles is reverse each other; The two ends of tubular shaft are equipped with the swivel joint that is connected with the thermal oil circulation line, form the circulation path by swivel joint and thermal oil vapour generator; Two offsides at cylindrical shell are provided with heat conductive oil inlet and the thermal oil outlet that communicates with the chuck chamber, and form the circulation path with the thermal oil vapour generator; The pump circulation of thermal oil is realized in the circulation path by Heat-transfer Oil Pump.
Trimeric cyanamide heat conducting oil energy-conserving production system of the present invention mainly is made of jointly Salt heater, fluidized-bed reactor, hot gas water cooler, hot gas purification device, hot gas crystallisation by cooling system, compressor and tail gas absorption system;
Above-mentioned hot gas crystallisation by cooling system is made up of thermal oil hollow blade crystallisation by cooling machine, electrostatic precipitator, thermal oil vapour generator and cyclonic separator; Its annexation is: thermal oil hollow blade crystallisation by cooling machine, cyclonic separator are connected successively with the hot gas purification device, and the thermal oil vapour generator is connected in parallel on the thermal oil import and export of thermal oil hollow blade crystallisation by cooling machine.
Above-mentioned hot gas purification device adopt that electrostatic precipitator or traditional technology use the hot gas filtration device all can.
Trimeric cyanamide heat conducting oil energy-conserving producing and manufacturing technique of the present invention is as follows:
The first step: the preparation of high temperature trimeric cyanamide mixed gas
According to prior art urea prepared in reaction in fluidized-bed reactor is become about 380 degrees centigrade the high temperature trimeric cyanamide mixed gas of being made up of trimeric cyanamide gas, ammonia and carbon dioxide gas;
Second step: the cooling and the purification of high temperature trimeric cyanamide mixed gas
The high temperature trimeric cyanamide mixed gas that will prepare from fluidized-bed reactor through the cooling of hot gas water cooler, refining plant filtration, purification, obtains warm mixed gas in pure about 320 degrees centigrade;
The 3rd step: the forced crystallization of middle temperature trimeric cyanamide mixed gas
Middle temperature trimeric cyanamide mixed gas sent in the thermal oil hollow blade crystallisation by cooling machine carry out heat exchange with thermal oil, the temperature of mixed gas is dropped to about 200 degrees centigrade, this moment, the trimeric cyanamide crystallization was separated out; Thermal oil after heat exchange simultaneously heats up enters the thermal oil vapour generator, cools to 140-150 degree centigrade after the soft water heat absorption, reenters thermal oil hollow blade crystallisation by cooling machine again by Heat-transfer Oil Pump and recycles;
The 4th step: the separation of trimeric cyanamide finished product
The ammonia of trimeric cyanamide crystallisate in mixed gas that crystallization is separated out in thermal oil hollow blade crystallisation by cooling machine enters cyclonic separator with carbon dioxide gas to be separated, and obtains the trimeric cyanamide finished product;
The 5th step: the recycling of low temperature ammonia and carbon dioxide gas
The ammonia that comes out from the cyclonic separator top and the mixed gas of carbon dioxide gas are through the further purification of electrostatic precipitator, reclaim out residual trimeric cyanamide finished product, pure mixed gas one small part of low temperature about all the other 200 degrees centigrade enters the tail gas absorption system and absorbs, most of cycles prepare that enters fluidized-bed participation trimeric cyanamide through compressor again.
The present invention can be used for carrying out cycles, economized combination producing trimeric cyanamide in synthetic ammonia soda ash production system or the synthetic ammonia carbon ammonium production system.Promptly the synthetic ammonia workshop section from synthetic ammonia soda ash production system or synthetic ammonia carbon ammonium production system directly is that the pure ammonia process gas of 0.1～0.2MPa is incorporated in the fluidized-bed reactor of production system of the present invention with pressure, produces trimeric cyanamide through producing and manufacturing technique of the present invention; Low-temperature mixed process gas after electrostatic precipitator purifies is sent into soda ash workshop section the synthetic ammonia soda ash production system or the carbon ammonium workshop section in the synthetic ammonia carbon ammonium production system again, use as the unstripped gas in producing, thus the combination producing pattern of the highly-efficient energy-saving low-carbon environmental protection of realization upstream and downstream resource circulation utilization.
Positively effect of the present invention is:
1, in the crystallisation by cooling process of trimeric cyanamide energy-saving processing technique of the present invention, adopts first to have thermal oil hollow blade crystallisation by cooling machine that movable heat-transfer surface and heat-transfer surface have a self-cleaning function and trimeric cyanamide is carried out crystallization reclaim; And adopting thermal oil first as trimeric cyanamide crystallization heat-eliminating medium, thermal oil produces steam to heat transferred soft water; The thermal oil closed cycle does not have heat an ancient egg-shaped, holed wind instrument consumption, has realized the high efficiente callback utilization of crystallisation by cooling waste heat, has saved the energy, has reduced consumption;
2, in the crystallisation by cooling process of trimeric cyanamide energy-saving processing technique of the present invention, adopt the simple combination of thermal oil hollow blade crystallisation by cooling machine, electrostatic precipitator and thermal oil vapour generator first, system device and the corresponding pipeline valves such as crystallizer, circulating cold air blower fan, liquid urine recycle pump, liquid urine washing tower, gas-liquid separator and liquid urine water cooler that have replaced numerous and diverse costliness in traditional normal, low pressure one-step technology have significantly reduced equipment, material and the supporting construction investment expense of device; Compare with traditional technology, the initial outlay expense can reduce by 50～60%;
3, trimeric cyanamide energy-saving processing technique of the present invention adopts electrostatic precipitator that warm trimeric cyanamide hybrid technique gas in 320 degrees centigrade and 200 degrees centigrade of low-temperature mixed process gas are purified first.Because of the resistance of the electrostatic precipitator resistance much smaller than the traditional hot air filter, the motor operating load of compressor just can reduce relatively, the effective like this power consumption that reduces compressor; Do not need regularly to switch because of electrostatic precipitator simultaneously, prolonged the cycle of operation of device greatly;
4, the low temperature process gas after trimeric cyanamide energy-saving processing technique of the present invention purifies directly circulates through compressor from 200 degrees centigrade, not needing to resemble traditional technology is reduced to 140 degrees centigrade and just circulates through compressor, so just, 2 * 60 degrees centigrade cooling and temperature-rise period have been saved, save 120 degrees centigrade heat energy, can reduce fuel consumption 30%;
5, trimeric cyanamide energy-saving processing technique of the present invention does not exist powerful circulating cold air blower fan and liquid urine recycle pump to carry out cold air and the circulation of liquid urine, has reduced the power consumption of half, greatly reduces the working cost of device; Compare with traditional technology, the integrated operation energy consumption can reduce by 60%;
6, trimeric cyanamide energy-saving processing technique of the present invention utilizes unique thermal oil forced crystallization mode, by the efficient comprehensive reutilization of optimization to traditional technology system heat energy, simplify greatly and shortened the numerous long complicated operational path of traditional technology, reduced a large amount of equipment input investments, can the automatization serialization produce, once go out finished product; Have the flow process weak point and gather, control easy, distinguishing features such as start-stop is flexible, reduced investment is little, energy consumption is low less, low-carbon environment-friendly, coproduction capable of circulation;
7, utilize trimeric cyanamide energy-saving processing technique of the present invention to carry out the energy saving technology transformation, make traditional technology be transformed into energy-saving technique under the investment situation spending seldom traditional normal pressure one, two-step process system; Particularly to traditional normal pressure two-step process, can realize that two-step approach changes single stage method: after the transformation not only waste heat carried out efficient recovery and realized energy-saving and cost-reducing, also variable batch production is continuous production, need make with extra care, and once goes out finished product etc., greatly reduces the energy consumption and the cost of device;
8, trimeric cyanamide energy-saving processing technique of the present invention: do not have the working cycle of liquid urine, can not carry liquid urine particulate in the process gas secretly, also do not have urea decomposition and produce part biuret phenomenon, reduced urea consumption; Equipment and pipeline do not need steam tracing, have reduced steam consumption; The flying away of triamine dust and surplus ammonia when not having discharging reduced supplies consumption and environmental pollution; Do not exist the trap outer wall has been carried out regularly having beaten and eliminated a series of traditional technologys such as noise pollution exist insoluble always not only having increased consumption but also the common problem of contaminate environment;
9, the present invention can carry out the upstream and downstream material with synthetic ammonia soda ash device or synthetic ammonia carbon ammonium device and utilizes each other, unites energy-conservation production trimeric cyanamide.This technology is simultaneously without three moving equipment of prominent high energy consumption in traditional trimeric cyanamide one-step technologies such as carrier gas compressor, circulating cold air blower fan, liquid urine recycle pump, power consumption can reduce more than 90%, can realize the efficient comprehensive cycling and reutilization of resource, thoroughly reach energy saving purposes.
Description of drawings:
Fig. 1 is that tradition is normal, low pressure single stage method Melamine Production system process figure;
Fig. 2 is traditional normal pressure two-step approach Melamine Production system process figure;
Fig. 3 is the energy-conservation production system artwork of the trimeric cyanamide of the embodiment of the invention one;
Fig. 4 is the energy-conservation production system artwork of the trimeric cyanamide of the embodiment of the invention two;
Fig. 5 is the energy-conservation combination producing system process of the trimeric cyanamide of the embodiment of the invention one figure;
Fig. 6 is the energy-conservation combination producing system process of the trimeric cyanamide of the embodiment of the invention two figure;
Fig. 7 is that thermal oil hollow blade crystallisation by cooling mechanism makes front view;
Fig. 8 is the structure vertical view of Fig. 7;
Fig. 9 is the A-A sectional drawing of Fig. 7;
Figure 10 is the structure front view of thermal oil hollow blade crystallisation by cooling machine another program;
Figure 11 is the structure vertical view of Figure 10;
Figure 12 is the A-A sectional drawing of Figure 10.
Marginal data: 1-cylindrical shell, 2-tubular shaft, 3-fan-shaped blade, 4-transmission mechanism, 5-swivel joint, 6-swivel joint, 7-combi inlet port, 8-mixture outlet, 9-heat conductive oil inlet, the outlet of 10-thermal oil, 11-scraper plate.
Embodiment
Fig. 1 is that tradition is normal, low pressure single stage method Melamine Production system process figure; Fig. 2 is traditional normal pressure two-step approach Melamine Production system process figure; Its concrete technology scape technology of passing away is described, is not described in detail in this.
The embodiment of the invention one; With reference to the accompanying drawings 3 and Fig. 5 the embodiment of energy-conservation production system of trimeric cyanamide thermal oil forced crystallization and energy-conservation combination producing system is further specified.
As Fig. 3, shown in Figure 5, trimeric cyanamide heat conducting oil energy-conserving production system of the present invention and energy-conservation combination producing system mainly are made of jointly Salt heater, fluidized-bed reactor, hot gas water cooler, hot gas purification device, hot gas crystallisation by cooling system, compressor and tail gas absorption system; Wherein the hot gas purification device adopts general electrostatic precipitator on the market.Above-mentioned hot gas crystallisation by cooling system mainly is made up of thermal oil hollow blade crystallisation by cooling machine, electrostatic precipitator, thermal oil vapour generator and cyclonic separator etc.
The embodiment of the invention two;
With reference to the accompanying drawings 4 and Fig. 6 the embodiment of energy-conservation production system of trimeric cyanamide thermal oil forced crystallization and energy-conservation combination producing system is further specified.
As Fig. 4, shown in Figure 6, trimeric cyanamide heat conducting oil energy-conserving production system of the present invention mainly is made of jointly Salt heater, fluidized-bed reactor, hot gas water cooler, hot gas purification device, hot gas crystallisation by cooling system, compressor and tail gas absorption system; Wherein the hot gas purification device adopts the hot gas filtration device that traditional technology is used.Above-mentioned hot gas crystallisation by cooling system mainly is made up of thermal oil hollow blade crystallisation by cooling machine, electrostatic precipitator, thermal oil vapour generator and cyclonic separator etc.
Thermal oil hollow blade crystallisation by cooling machine described in the embodiment one, two be configured with two kinds of makes.
First kind of make is shown in Fig. 7,8,9: it comprises a chuck shape cylindrical shell 1, and an end top of cylindrical shell is provided with the combi inlet port 7, the other end bottom that link to each other with the outlet of hot gas purification device and is provided with the mixture outlet 8 that links to each other with cyclonic separator; Two to four tubular shafts 2 are installed on the axis plane in cylindrical shell; All be furnished with fan-shaped blade 3 staggered arrangement of fan-shaped blade 3, the two adjacent vacant axles of hollow on every tubular shaft 2 at interval; The cavity of fan-shaped blade 3 communicates with the cavity of tubular shaft 2; Be fixed with spaced apart scraper plate 11 on cylindrical shell 1 inwall, scraper plate 11 stretches between two fan-shaped blades 3, guarantees that all fan-shaped blade both sides all are furnished with scraper plate, and scraper plate 11 is the 6-10 millimeter with the mutual gap of fan-shaped blade 3; Tubular shaft 2 rotates with the lower velocity that per minute 3 to 18 changes by transmission mechanism 4, and the turning direction of two adjacent vacant axles is reverse each other; The two ends of tubular shaft 2 are equipped with swivel joint 5 and the swivel joint 6 that is connected with the thermal oil circulation line, form the circulation path by swivel joint and thermal oil vapour generator; Two offsides at cylindrical shell 1 are provided with heat conductive oil inlet 9 and the thermal oil outlet 10 that communicates with the chuck chamber, and form the circulation path with the thermal oil vapour generator; The pump circulation of thermal oil is realized in the circulation path by Heat-transfer Oil Pump.
Second kind of make is shown in Figure 10,11,12, and it is identical with first kind of make, only is that the fan-shaped blade 3 of two adjacent vacant axles adopts the positioned opposite mode.
With reference to the accompanying drawings 3 and Fig. 4 trimeric cyanamide thermal oil forced crystallization energy-saving production method embodiment is further specified.
The first step: the preparation of high temperature trimeric cyanamide mixed gas
According to prior art urea prepared in reaction in fluidized-bed reactor is become about 380 degrees centigrade the high temperature trimeric cyanamide mixed gas of being made up of trimeric cyanamide gas, ammonia and carbon dioxide gas;
Second step: the cooling and the purification of high temperature trimeric cyanamide mixed gas
The high temperature trimeric cyanamide mixed gas that will prepare from fluidized-bed reactor through the cooling of hot gas water cooler, refining plant filtration, purification, obtains warm mixed gas in pure about 320 degrees centigrade;
The 3rd step: the forced crystallization of middle temperature trimeric cyanamide mixed gas
Middle temperature trimeric cyanamide mixed gas sent in the thermal oil hollow blade crystallisation by cooling machine carry out heat exchange with thermal oil, the temperature of mixed gas is dropped to about 200 degrees centigrade, this moment, the trimeric cyanamide crystallization was separated out; Thermal oil after heat exchange simultaneously heats up enters the thermal oil vapour generator, cools to 140-150 degree centigrade after the soft water heat absorption, reenters thermal oil hollow blade crystallisation by cooling machine again by Heat-transfer Oil Pump and recycles;
The 4th step: the separation of trimeric cyanamide finished product
The ammonia of trimeric cyanamide crystallisate in mixed gas that crystallization is separated out in thermal oil hollow blade crystallisation by cooling machine enters cyclonic separator with carbon dioxide gas to be separated, and obtains the trimeric cyanamide finished product;
The 5th step: the recycling of low temperature ammonia and carbon dioxide gas
The ammonia that comes out from the cyclonic separator top and the mixed gas of carbon dioxide gas are through the further purification of electrostatic precipitator, reclaim out residual trimeric cyanamide finished product, pure mixed gas one small part of low temperature about all the other 200 degrees centigrade enters the tail gas absorption system and absorbs, most of cycles prepare that enters fluidized-bed participation trimeric cyanamide through compressor again.
As Fig. 5, shown in Figure 6, the present invention can be used for carrying out cycles, economized combination producing trimeric cyanamide in synthetic ammonia soda ash production system or the synthetic ammonia carbon ammonium production system.Promptly the synthetic ammonia workshop section from synthetic ammonia soda ash production system or synthetic ammonia carbon ammonium production system directly is that the pure ammonia process gas of 0.1～0.2MPa is incorporated in the fluidized-bed reactor of production system of the present invention with pressure, produces trimeric cyanamide through producing and manufacturing technique of the present invention; Low-temperature mixed process gas after electrostatic precipitator purifies is sent into soda ash workshop section the synthetic ammonia soda ash production system or the carbon ammonium workshop section in the synthetic ammonia carbon ammonium production system again, recycle as raw materials for production gas, thus the combination producing pattern of the highly-efficient energy-saving low-carbon environmental protection of realization upstream and downstream resource circulation utilization.
Claims (4)
1. thermal oil hollow blade crystallisation by cooling machine, it is characterized in that, it comprises a chuck shape cylindrical shell, and an end top of cylindrical shell is provided with the combi inlet port, the other end bottom that link to each other with the outlet of hot gas purification device and is provided with the mixture outlet that links to each other with cyclonic separator; Two to four tubular shafts are installed on the axis plane in cylindrical shell; All be furnished with the fan-shaped blade of hollow on every tubular shaft at interval, the fan-shaped blade positioned opposite or the staggered arrangement of two adjacent vacant axles; The cavity of fan-shaped blade communicates with the cavity of tubular shaft; Be fixed with spaced apart scraper plate on cylinder inboard wall, scraper plate stretches between the fan-shaped blade, guarantees that all fan-shaped blade both sides all are furnished with scraper plate, and the mutual gap of scraper plate and fan-shaped blade is the 6-10 millimeter; Tubular shaft rotates with the lower velocity that per minute 3 to 18 changes by transmission mechanism, and the turning direction of two adjacent vacant axles is reverse each other; The two ends of tubular shaft are equipped with the swivel joint that is connected with the thermal oil circulation line, form the circulation path by swivel joint and thermal oil vapour generator; Two offsides at cylindrical shell are provided with heat conductive oil inlet and the thermal oil outlet that communicates with the chuck chamber, and form the circulation path with the thermal oil vapour generator; The pump circulation of thermal oil is realized in the circulation path by Heat-transfer Oil Pump.
2. a trimeric cyanamide heat conducting oil energy-conserving production system of being made up of the described crystallisation by cooling machine of claim 1 mainly is made of jointly Salt heater, fluidized-bed reactor, hot gas water cooler, hot gas purification device, hot gas crystallisation by cooling system, compressor and tail gas absorption system; It is characterized in that: above-mentioned hot gas crystallisation by cooling system is made up of thermal oil hollow blade crystallisation by cooling machine, hot gas purification device, thermal oil vapour generator and cyclonic separator; Its annexation is: thermal oil hollow blade crystallisation by cooling machine, cyclonic separator are connected successively with the hot gas purification device, and the thermal oil vapour generator is connected in parallel on the thermal oil import and export of thermal oil hollow blade crystallisation by cooling machine.
3. production system as claimed in claim 2 is characterized in that: described hot gas purification device adopts electrostatic precipitator or hot gas filtration device.
4. one kind is utilized claim 2 or method that 3 described systems produce trimeric cyanamides, it is characterized in that step is as follows:
The first step: the preparation of high temperature trimeric cyanamide mixed gas
One of following three kinds of modes are adopted in the preparation of trimeric cyanamide mixed gas:
The one: according to prior art urea prepared in reaction in fluidized-bed reactor is become 380 degrees centigrade the high temperature trimeric cyanamide mixed gas of being made up of trimeric cyanamide gas, ammonia and carbon dioxide gas;
The 2nd: with the pressure of the synthetic ammonia workshop section output in the synthetic ammonia carbon ammonium production system is that the pure ammonia process gas of 0.1～0.2MPa is incorporated in the fluidized-bed reactor, makes 380 degrees centigrade high temperature trimeric cyanamide mixed gas;
The 3rd: with the pressure of the synthetic ammonia workshop section output in the synthetic ammonia soda ash production system is that the pure ammonia process gas of 0.1～0.2MPa is incorporated in the fluidized-bed reactor, makes 380 degrees centigrade high temperature trimeric cyanamide mixed gas;
Second step: the cooling and the purification of high temperature trimeric cyanamide mixed gas
The high temperature trimeric cyanamide mixed gas that will prepare from fluidized-bed reactor through the cooling of hot gas water cooler, refining plant filtration, purification, obtains warm mixed gas in 320 degrees centigrade pure;
The 3rd step: the forced crystallization of middle temperature trimeric cyanamide mixed gas
Middle temperature trimeric cyanamide mixed gas sent in the thermal oil hollow blade crystallisation by cooling machine carry out heat exchange with thermal oil, make the temperature of mixed gas drop to 200 degrees centigrade, this moment, the trimeric cyanamide crystallization was separated out; Thermal oil after heat exchange simultaneously heats up enters the thermal oil vapour generator, cools to 140-150 degree centigrade after the soft water heat absorption,
The 4th step: the separation of trimeric cyanamide finished product
The ammonia of trimeric cyanamide crystallisate in mixed gas that crystallization is separated out in thermal oil hollow blade crystallisation by cooling machine enters cyclonic separator with carbon dioxide gas to be separated, and obtains the trimeric cyanamide finished product;
The 5th step: the recycling of low temperature ammonia and carbon dioxide gas
The ammonia that comes out from the cyclonic separator top and the mixed gas of carbon dioxide gas are through the further purification of electrostatic precipitator, reclaim out residual trimeric cyanamide finished product, the pure mixed gas part of all the other low temperature of 200 degrees centigrade enters the tail gas absorption system and absorbs, and remainder returns the first step again and recycles as unstripped gas.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102514938A (en) * | 2012-01-06 | 2012-06-27 | 中冶东方工程技术有限公司 | Indirect-heat-exchange cooling system and cooling method thereof |
| CN103102320A (en) * | 2013-01-17 | 2013-05-15 | 李鑫 | Production method of melamine by slow cooling crystallization |
| CN104235810A (en) * | 2014-09-08 | 2014-12-24 | 山东省舜天化工集团有限公司 | Heat energy recovery device for heat energy produced based on melamine |
| CN104315871A (en) * | 2014-10-30 | 2015-01-28 | 安徽金禾实业股份有限公司 | Molten-salt-furnace outlet flue gas heat energy recovery method in melamine production |
| CN105061344A (en) * | 2015-08-09 | 2015-11-18 | 李东田 | Melamine slow-cooling crystallization production method |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202107649U (en) * | 2011-05-08 | 2012-01-11 | 徐建华 | Production device for melamine and energy-saving production system |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5787801A (en) * | 1980-11-19 | 1982-06-01 | Kureha Chem Ind Co Ltd | Crystal refining device |
| JPH0240204A (en) * | 1988-07-27 | 1990-02-09 | Nagano Pref Gov Nouson Kogyo Kenkyusho | Device for freezing and concentrating solution |
| EP0446381A1 (en) * | 1989-10-04 | 1991-09-18 | Shigeru Saitoh | Crystal refining apparatus |
| CN1180699A (en) * | 1997-09-19 | 1998-05-06 | 河北省广平县化肥厂 | Technology for producing ammonium carbonate with combined production of melamine |
| CN1493565A (en) * | 2003-09-17 | 2004-05-05 | 丁泽华 | Trimeric cyanamide joint production method using one step method |
| CN1493383A (en) * | 2002-11-01 | 2004-05-05 | 月岛机械株式会社 | Circulation of liquid to be processed type scraping crystallization device |
| CN200949989Y (en) * | 2006-09-13 | 2007-09-19 | 许建庄 | Multi-layer paddle drying machine |
| CN101216243A (en) * | 2008-01-09 | 2008-07-09 | 浙江大学 | System for drying sludge by solar energy |
| CN202107649U (en) * | 2011-05-08 | 2012-01-11 | 徐建华 | Production device for melamine and energy-saving production system |
-
2011
- 2011-06-28 CN CN201120221652XU patent/CN202107649U/en not_active Expired - Lifetime
- 2011-06-28 CN CN2011101761025A patent/CN102276544B/en not_active Expired - Fee Related
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5787801A (en) * | 1980-11-19 | 1982-06-01 | Kureha Chem Ind Co Ltd | Crystal refining device |
| JPH0240204A (en) * | 1988-07-27 | 1990-02-09 | Nagano Pref Gov Nouson Kogyo Kenkyusho | Device for freezing and concentrating solution |
| EP0446381A1 (en) * | 1989-10-04 | 1991-09-18 | Shigeru Saitoh | Crystal refining apparatus |
| CN1180699A (en) * | 1997-09-19 | 1998-05-06 | 河北省广平县化肥厂 | Technology for producing ammonium carbonate with combined production of melamine |
| CN1493383A (en) * | 2002-11-01 | 2004-05-05 | 月岛机械株式会社 | Circulation of liquid to be processed type scraping crystallization device |
| CN1493565A (en) * | 2003-09-17 | 2004-05-05 | 丁泽华 | Trimeric cyanamide joint production method using one step method |
| CN200949989Y (en) * | 2006-09-13 | 2007-09-19 | 许建庄 | Multi-layer paddle drying machine |
| CN101216243A (en) * | 2008-01-09 | 2008-07-09 | 浙江大学 | System for drying sludge by solar energy |
| CN202107649U (en) * | 2011-05-08 | 2012-01-11 | 徐建华 | Production device for melamine and energy-saving production system |
Non-Patent Citations (1)
| Title |
|---|
| 吴伟成等: "空心桨叶干燥器的研究开发及应用", 《浙江化工》, no. 9, 30 September 2004 (2004-09-30) * |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102514938A (en) * | 2012-01-06 | 2012-06-27 | 中冶东方工程技术有限公司 | Indirect-heat-exchange cooling system and cooling method thereof |
| CN103102320A (en) * | 2013-01-17 | 2013-05-15 | 李鑫 | Production method of melamine by slow cooling crystallization |
| CN104235810A (en) * | 2014-09-08 | 2014-12-24 | 山东省舜天化工集团有限公司 | Heat energy recovery device for heat energy produced based on melamine |
| CN104315871A (en) * | 2014-10-30 | 2015-01-28 | 安徽金禾实业股份有限公司 | Molten-salt-furnace outlet flue gas heat energy recovery method in melamine production |
| CN104315871B (en) * | 2014-10-30 | 2016-05-25 | 安徽金禾实业股份有限公司 | Molten salt furnace outlet smoke heat energy recovery method in Melamine Production |
| CN105061344A (en) * | 2015-08-09 | 2015-11-18 | 李东田 | Melamine slow-cooling crystallization production method |
| CN105061344B (en) * | 2015-08-09 | 2017-09-22 | 李东田 | A kind of melamine slow cooling crystallizes production method |
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| CN202107649U (en) | 2012-01-11 |
| CN102276544B (en) | 2013-10-16 |
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