CN102584730A - Equipment and process for producing melamine under low pressure - Google Patents
Equipment and process for producing melamine under low pressure Download PDFInfo
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- CN102584730A CN102584730A CN2012100616368A CN201210061636A CN102584730A CN 102584730 A CN102584730 A CN 102584730A CN 2012100616368 A CN2012100616368 A CN 2012100616368A CN 201210061636 A CN201210061636 A CN 201210061636A CN 102584730 A CN102584730 A CN 102584730A
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Abstract
The invention discloses equipment and a process for producing melamine under a low pressure. The process comprises the following steps of: (1) atomizing molten urea, introducing into a reactor, and reacting by taking gas ammonia as a reaction carrier gas in a reactor under the condition that the temperature is 380-410 DEG C and the pressure is 0.1-1.4MPa to generate melamine, carbon dioxide, ammonia and a deamination product of melamine; (2) after reacting, crystalizing the deamination product, filtering, cooling the filtered gas with a quenching medium, and separating to obtain a finished product; (3) absorbing the gas left after separation with water to form a methylamine solution and a mixed gas; and (4) rectifying the mixed gas under the condition that the temperature is between 30 DEG C below zero and 30 DEG C to form ammonia gas, and returning the ammonia gas to the step (1) for serving as a reaction carrier gas or/and returning to the step (2) for serving as quenching medium. The invention further discloses equipment for producing melamine under a low pressure. The equipment and the process have the advantages of good product quality, high production efficiency, low energy consumption, environmental friendliness, simple process, and the like.
Description
Technical field
What the present invention relates to is a kind of Production of Cyanuramide technology, and what be specifically related to is the technology that low pressure is produced trimeric cyanamide, the invention still further relates to the equipment that low pressure is produced trimeric cyanamide.
Background technology
The Production of Cyanuramide flow process all includes three master operations such as polyreaction, quenching separation and vent gas treatment usually.
Polyreaction: with urea is raw material, under certain temperature, pressure, is converted into trimeric cyanamide, emits NH simultaneously
3And CO
2
Quenching separates: be divided into liquid phase quenching method and gas phase quenching method.The common water of liquid phase quenching method or contain the aqueous solution quenching reaction product of trimeric cyanamide is dissolved in the aqueous solution trimeric cyanamide fully, or is partly dissolved partial crystallization and separates out; The gas phase quenching method is usually with containing NH
3And CO
2Mixed gas quenching reaction product, trimeric cyanamide is crystallized out from gas phase.
Vent gas treatment: behind the ammonia of by-product and carbonic acid gas and the product separation, liquid phase quenching technology adopts the mode of condensed and absorbed to process first ammonium solution carrying device usually, or recovery part ammonia recycles; Gas phase quenching technology generally is to extract a part of water out to absorb into first ammonium solution or direct carrying device, and rest part is at system's internal recycle.
The problem of the low pressure liquid phase quenching method of common trimeric cyanamide is: technical process is long, complicated operation; Equipment is many, and volume is relatively large, and equipment component requires high to material, invest bigger; Product purifies to be needed to consume steam, and energy consumption is higher; Tail gas pressure is low and contain large quantity of moisture etc., is difficult for directly utilizing; The strainer filter residue is difficult to handle, and has environmental protection hidden danger.
The problem of low-pressure vapor phase quenching method is: quenching gas needs with the fusing urea washing, thereby the urea mist of carrying secretly is prone to fouling block system in process line, influences long-term operation; Reactant gases is because of being entrained with by product and catalyzer, the easy blocking interchanger; Need to be equipped with and to bear comparatively high temps, powerful compressor unit; Tail gas is low because of pressure, handles comparatively difficulty.
Summary of the invention
The object of the present invention is to provide the technology that a kind of technology is simple, quality product is excellent, production efficiency is high, energy consumption is low, free of contamination low pressure is produced trimeric cyanamide.
Realize that technical scheme of the present invention is following: low pressure is produced the equipment of trimeric cyanamide; Mainly constitute, also be connected with exhaust fan, preheater, ammonia absorber on the said separator in order by the reactor drum, strainer, quencher, tripping device and the intermediates groove that connect in order; The top of said ammonia absorber is connected with reactor drum with preheater through compressor, and said ammonia absorber top and ammonia compressor, ammonia cooler, ammonia storage tank and boosting pump are connected to form loop structure in order.
Further, the top of said ammonia absorber is connected with quencher or said boosting pump is connected with quencher.
Further, said ammonia absorber bottom and recycle pump and water cooler are connected to form loop structure in order.
As a kind of preferred, said tripping device is cyclonic separator or strainer.
Low pressure is produced the technology of trimeric cyanamide, mainly is made up of following steps:
(1) fusing urea gets into reactor drum after atomizing; As the reaction carrier gas, is that 380 ℃～410 ℃, pressure be deamination product that the condition of 0.1MPa～1.4MPa under reaction generate trimeric cyanamide, carbonic acid gas, ammonia and trimeric cyanamide at reactor temperature with gas ammonia;
(2) after reaction was accomplished, crystallization deamination product also filtered, and the gas after the filtration is processed finished product after cooling off, separate through quenching medium;
(3) remaining gas water absorbs back formation first ammonium solution and mixed gas after the above-mentioned separation;
(4) rectifying under-30 ℃～30 ℃ condition of above-mentioned mixed gas forms ammonia, and said ammonia returns step (1) do reaction carrier gas Huo ∕ and returns step (2) and make quenching medium.
Further, the rectifying of above-mentioned mixed gas is to reduce the mixed gas method of temperature through the low temperature gas ammonia to realize.
As a kind of preferred, the Tc of deamination product is 340 ℃～380 ℃ in the above-mentioned steps (2).
For more crystalline goes out melamine crystals, cooling temperature is 100 ℃～200 ℃ in the above-mentioned steps (2).
In order to practice thrift cost, filtering product in the above-mentioned steps (2) blows Returning reactor with hot ammonia.
As the embodiment of optimum, said quenching medium is an ammonia.
The present invention has the following advantages and beneficial effect:
1, the present invention uses gas ammonia as the reaction carrier gas, as carrier gas, has reduced the gas circulation amount than the gas mixture that uses ammonia and carbonic acid gas, has practiced thrift the carrier gas energy consumption of compressor, has also reduced the heat that offers reactor drum simultaneously;
2, after the present invention adopts ammonia as quenching gas; Having avoided the available technology adopting mixed gas to make quenching gas needs to wash tower with fusing urea washing cooling at urine earlier; Possibly take urea droplets out of, cause the knot wall and the blocking problem of pipeline, equipment, but significant prolongation continuous apparatus working time;
3, the present invention uses ammonia as quenching gas, can reduce air conditioning quantity significantly, practices thrift the cold air fan energy consumption;
4, the present invention is higher because of the ammonia dividing potential drop in the reactor drum, so can reduce the generation of deamination product, improves product purity;
5, the by product taken out of of reactant gases of the present invention uses at system's internal recycle after separating, and cuts down the consumption of energy the purpose of aggrandizement apparatus throughput thereby the present invention is reached;
6, the present invention adopts low temperature gas ammonia reduction mixed gas method of temperature that mixed gas is carried out rectifying, can reduce energy consumption greatly, practices thrift cost;
7, reactant gases of the present invention is all recycled, and does not have other refuses and discharges, and whole process safety is pollution-free;
8, technology of the present invention is simple, and is with low cost, is suitable for promoting.
Description of drawings
Fig. 1 is the system flow synoptic diagram of embodiment 1 and embodiment 2.
Fig. 2 is the system flow synoptic diagram of embodiment 3.
Wherein, the component name that Reference numeral is corresponding among the figure is called:
The 1-reactor drum, 2-strainer, 3-quencher, 4-first cyclonic separator; 5-second cyclonic separator, 6-intermediates groove, 7-ammonia absorber, 8-exhaust fan; The 9-preheater, 10-recycle pump, 11-water cooler, 12-ammonia storage tank; The 13-ammonia compressor, 14-ammonia cooler, 15-boosting pump.
Embodiment
Below in conjunction with accompanying drawing and embodiment the present invention is described further, but embodiment of the present invention is not limited thereto.
Embodiment 1
As shown in Figure 1, low pressure is produced the technology of trimeric cyanamide, mainly is made up of following steps.
At first; To add in the reactor drum 1 through the fusing urea after the atomizing, and use gas ammonia to feed in the reactor drum as the reaction carrier gas, fused salt provides heat of reaction through the heating coil that is positioned at reactor drum 1; And keep in the reactor drum 1 temperature in 380 ℃, be to react under the condition of 0.3MPa in reaction pressure.
Urea generates trimeric cyanamide, by-product carbonic acid gas and ammonia at reactor drum 1 internal reaction, has a spot of trimeric cyanamide further to react the deamination product that generates trimeric cyanamide simultaneously.Under this temperature of reaction, ammonia, carbonic acid gas, trimeric cyanamide, deamination product are gaseous state.
What reactor drum 1 of the present invention adopted is fluidized-bed reactor.In order to be beneficial to reaction, also added catalyst in the said reaction process, the kind of this catalyst is all identical with consumption with the employed conventional kind of urea production trimeric cyanamide with those skilled in the art with usage quantity.
Secondly, after reaction is accomplished, reduce the temperature to 340 ℃, the deamination product will be separated out from gas phase in crystallization this moment.The gas that will contain deamination product crystal and catalyst filters through strainer 2, and just separate deamination product crystal and catalyst this moment from gas phase.
After strainer 2 has moved the certain hour differential pressure and has been elevated to a certain degree; Use temperature is that 390 ℃ high temperature gas ammonia carries out blowback to strainer 2; Catalyst that adheres on the strainer and deamination product are sent back in the reactor drum 1 by blowback air, thereby recover the effect of strainer 2 and can effectively reduce the loss of raw material.
Gas after the filtration feeds in the quencher 3, in quencher 3, sprays into the low temperature gas ammonia simultaneously, uses the gas temperature after the low temperature gas ammonia will filter to reduce to 140 ℃, and at this moment, the trimeric cyanamide Yin Wendu in gas phase reduces and crystallization.
Once more; The reactant gases that will contain melamine crystals feeds first cyclonic separator 4 to be separated; Isolated melamine crystals is introduced intermediates groove 6; Isolated gas then separates through second cyclonic separator 5 once more, reaches the purpose of from gas phase, isolating melamine crystals through the isolating mode of two stage cyclone.To introduce in the intermediates groove 6 through second cyclonic separator, 5 isolated melamine crystals, and separate the remaining gas in back and then recycle.Second cyclonic separator 5 in the present embodiment can replace with deep bed filter, and this mode also can reach the purpose of from gas phase, isolating melamine crystals.
The melamine crystals that feeds in the intermediates groove 6 is sent to the finished product storage tank after handling.
Separate the remaining gas in back in the above step and find through detecting, the gaseous ammonia very high concentrations contains 85%～95% ammonia and 5%～15% carbonic acid gas in the gas, and the rare gas element of trace.
After recovery gas passes through exhaust fan 8 and preheater 9; Feed ammonia absorber 7 bottoms; Through water absorbing carbon dioxide and the part ammonia that adds from ammonia absorber 7 middle parts, the material with water absorbing carbon dioxide in the ammonia absorber 7 and the formation of part ammonia constantly loops back in the inflow ammonia absorber 7 through recycle pump 10 and water cooler 11 then.After the material concentration that forms reaches 50%, discharge, the material of discharge is the first ammonium solution.
Rectifying is carried out at the top that remaining gas is then sent into ammonia absorber 7 in the ammonia absorber 7; Gas is divided into three the tunnel after the rectifying; One the tunnel directly feeds quencher 3 does the quenching medium use; Another road then feeds in the reactor drums 1 as the reaction carrier gas through compressor with preheater 9 back, and Third Road is transformed into liquefied ammonia through behind ammonia compressor 13 and the ammonia cooler 14, and this liquefied ammonia is back in the ammonia storage tank 12.The forming process of reaction carrier gas is following: through compressor compresses, the compression back is through preheater 9 and second cyclonic separator, 5 isolated gas converting heats with the gas after the rectifying, and gas just feeds in the reactor drum 1 as the reaction carrier gas after the heat exchange.
These ammonia absorber 7 top rectifying be through temperature reduction way to its rectifying, temperature is reduced to-18 ℃.The embodiment of present embodiment is following: the top that the liquefied ammonia in the ammonia storage tank 12 is fed ammonia absorber 7 through boosting pump 15 backs; The low temperature gas ammonia that liquefied ammonia volatilization back forms carries out freezing to the gas at top; Freezing back expellant gas is ammonia, and its purity can reach more than 99.5%.
Embodiment 2
As shown in Figure 1, low pressure is produced the technology of trimeric cyanamide, mainly is made up of following steps.
At first; To add in the reactor drum 1 through the fusing urea after the atomizing, and use gas ammonia to feed in the reactor drum as the reaction carrier gas, fused salt provides heat of reaction through the heating coil that is positioned at reactor drum 1; And keep in the reactor drum 1 temperature in 385 ℃, be to react under the condition of 0.6MPa in reaction pressure.
Urea generates trimeric cyanamide, by-product carbonic acid gas and ammonia at reactor drum 1 internal reaction, has a spot of trimeric cyanamide further to react the deamination product that generates trimeric cyanamide simultaneously.Under this temperature of reaction, ammonia, carbonic acid gas, trimeric cyanamide, deamination product are gaseous state.
What reactor drum 1 of the present invention adopted is fluidized-bed reactor.In order to be beneficial to reaction, also added catalyst in the said reaction process, the kind of this catalyst is all identical with consumption with the employed conventional kind of urea production trimeric cyanamide with those skilled in the art with usage quantity.
Secondly, after reaction is accomplished, reduce the temperature to 350 ℃, the deamination product will be separated out from gas phase in crystallization this moment.The gas that will contain deamination product crystal and catalyst filters through strainer 2, and just separate deamination product crystal and catalyst this moment from gas phase.
After strainer 2 has moved the certain hour differential pressure and has been elevated to a certain degree; Use temperature is that 390 ℃ high temperature gas ammonia carries out blowback to strainer 2; Catalyst that adheres on the strainer and deamination product are sent back in the reactor drum 1 by blowback air, thereby recover the effect of strainer 2 and can effectively reduce the loss of raw material.
Gas after the filtration feeds in the quencher 3, in quencher 3, sprays into the low temperature gas ammonia simultaneously, uses the gas temperature after the low temperature gas ammonia will filter to reduce to 140 ℃, and at this moment, the trimeric cyanamide Yin Wendu in gas phase reduces and crystallization.
Once more; The reactant gases that will contain melamine crystals feeds first cyclonic separator 4 to be separated; Isolated melamine crystals is introduced intermediates groove 6; Isolated gas then separates through second cyclonic separator 5 once more, reaches the purpose of from gas phase, isolating melamine crystals through the isolating mode of two stage cyclone.To introduce in the intermediates groove 6 through second cyclonic separator, 5 isolated melamine crystals, and separate the remaining gas in back and then recycle.Second cyclonic separator 5 in the present embodiment can replace with deep bed filter, and this mode also can reach the purpose of from gas phase, isolating melamine crystals.
The melamine crystals that feeds in the intermediates groove 6 is sent to the finished product storage tank after handling.
Separate the remaining gas in back in the above step and find through detecting, the gaseous ammonia very high concentrations contains 85%～95% ammonia and 5%～15% carbonic acid gas in the gas, and the rare gas element of trace.
After recovery gas passes through exhaust fan 8 and preheater 9; Feed ammonia absorber 7 bottoms; Through water absorbing carbon dioxide and the part ammonia that adds from ammonia absorber 7 middle parts, the material with water absorbing carbon dioxide in the ammonia absorber 7 and the formation of part ammonia constantly loops back in the inflow ammonia absorber 7 through recycle pump 10 and water cooler 11 then.After the material concentration that forms reaches 60%, discharge, the material of discharge is the first ammonium solution.
Rectifying is carried out at the top that remaining gas is then sent into ammonia absorber 7 in the ammonia absorber 7; Gas is divided into three the tunnel after the rectifying; One the tunnel directly feeds quencher 3 does the quenching medium use; Another road then feeds in the reactor drums 1 as the reaction carrier gas through compressor with preheater 9 back, and Third Road is transformed into liquefied ammonia through behind ammonia compressor 13 and the ammonia cooler 14, and this liquefied ammonia is back in the ammonia storage tank 12.The forming process of reaction carrier gas is following: through compressor compresses, the compression back is through preheater 9 and second cyclonic separator, 5 isolated gas converting heats with the gas after the rectifying, and gas just feeds in the reactor drum 1 as the reaction carrier gas after the heat exchange.
These ammonia absorber 7 top rectifying be through temperature reduction way to its rectifying, temperature is reduced to-2 ℃.The embodiment of present embodiment is following: the top that the liquefied ammonia in the ammonia storage tank 12 is fed ammonia absorber 7 through boosting pump 15 backs; The low temperature gas ammonia that liquefied ammonia volatilization back forms carries out freezing to the gas at top; Freezing back expellant gas is ammonia, and its purity can reach more than 99.5%.
Embodiment 3
As shown in Figure 2, low pressure is produced the technology of trimeric cyanamide, mainly is made up of following steps.
At first; To add in the reactor drum 1 through the fusing urea after the atomizing, and use gas ammonia to feed in the reactor drum as the reaction carrier gas, fused salt provides heat of reaction through the heating coil that is positioned at reactor drum 1; And keep in the reactor drum 1 temperature in 390 ℃, be to react under the condition of 1.2MPa in reaction pressure.
Urea generates trimeric cyanamide, by-product carbonic acid gas and ammonia at reactor drum 1 internal reaction, has a spot of trimeric cyanamide further to react the deamination product that generates trimeric cyanamide simultaneously.Under this temperature of reaction, ammonia, carbonic acid gas, trimeric cyanamide, deamination product are gaseous state.
What reactor drum 1 of the present invention adopted is fluidized-bed reactor.In order to be beneficial to reaction, also added catalyst in the said reaction process, the kind of this catalyst is all identical with consumption with the employed conventional kind of urea production trimeric cyanamide with those skilled in the art with usage quantity.
Secondly, after reaction is accomplished, reduce the temperature to 360 ℃, the deamination product will be separated out from gas phase in crystallization this moment.The gas that will contain deamination product crystal and catalyst filters through strainer 2, and just separate deamination product crystal and catalyst this moment from gas phase.
After strainer 2 has moved the certain hour differential pressure and has been elevated to a certain degree; Use temperature is that 390 ℃ high temperature gas ammonia carries out blowback to strainer 2; Catalyst that adheres on the strainer and deamination product are sent back in the reactor drum 1 by blowback air, thereby recover the effect of strainer 2 and can effectively reduce the loss of raw material.
Gas after the filtration feeds in the quencher 3, in quencher 3, sprays into liquefied ammonia simultaneously, and the gas temperature after filtering is reduced to 140 ℃, and at this moment, the trimeric cyanamide Yin Wendu in gas phase reduces and crystallization.
Once more; The reactant gases that will contain melamine crystals feeds first cyclonic separator 4 to be separated; Isolated melamine crystals is introduced intermediates groove 6; Isolated gas then separates through second cyclonic separator 5 once more, reaches the purpose of from gas phase, isolating melamine crystals through the isolating mode of two stage cyclone.To introduce in the intermediates groove 6 through second cyclonic separator, 5 isolated melamine crystals, and separate the remaining gas in back and then recycle.Second cyclonic separator 5 in the present embodiment can replace with deep bed filter, and this mode also can reach the purpose of from gas phase, isolating melamine crystals.
The melamine crystals that feeds in the intermediates groove 6 is sent to the finished product storage tank after handling.
Separate the remaining gas in back in the above step and find through detecting, the gaseous ammonia very high concentrations contains 85%～95% ammonia and 5%～15% carbonic acid gas in the gas, and the rare gas element of trace.
After recovery gas passes through exhaust fan 8 and preheater 9; Feed ammonia absorber 7 bottoms; Through water absorbing carbon dioxide and the part ammonia that adds from ammonia absorber 7 middle parts, the material with water absorbing carbon dioxide in the ammonia absorber 7 and the formation of part ammonia constantly loops back in the inflow ammonia absorber 7 through recycle pump 10 and water cooler 11 then.After the material concentration that forms reaches 70%, discharge, the material of discharge is the first ammonium solution.
Rectifying is carried out at the top that remaining gas is then sent into ammonia absorber 7 in the ammonia absorber 7; Gas is divided into two-way after the rectifying; Lead up to compressor and feed in the reactor drums 1 as the reaction carrier gas with preheater 9 back; Another road is transformed into liquefied ammonia through behind ammonia compressor 13 and the ammonia cooler 14, and this liquefied ammonia is back in the ammonia storage tank 12.The forming process of reaction carrier gas is following: through compressor compresses, the compression back is through preheater 9 and second cyclonic separator, 5 isolated gas converting heats with the gas after the rectifying, and gas just feeds in the reactor drum 1 as the reaction carrier gas after the heat exchange.Liquefied ammonia after boosting through boosting pump 15 in the ammonia storage tank 12 in the present embodiment sprays in the quencher 3 makes quenching medium.
These ammonia absorber 7 top rectifying be through temperature reduction way to its rectifying, temperature is reduced to 24 ℃.The embodiment of present embodiment is following: the top that the liquefied ammonia in the ammonia storage tank 12 is fed ammonia absorber 7 through boosting pump 15 backs; The low temperature gas ammonia that liquefied ammonia volatilization back forms carries out freezing to the gas at top; Freezing back expellant gas is ammonia, and its purity can reach more than 99.5%.
Compare according to above embodiment and common technology, its each item loss detected detected result such as following table 1:
Table 1
| ? | Common technology | Embodiment 1 | Embodiment 2 | Embodiment 3 |
| Reactor pressure (MPa) | 0.2 | 0.3 | 0.6 | 1.2 |
| Urea (t/t) | 3.05 | 2.95 | 2.95 | 2.95 |
| Load volume (t/t) | 9.5 | 3.0 | 3.0 | 3.0 |
| Fuel (Gcal/t) | 3.3 | 2.4 | 2.4 | 2.4 |
| Quenching tolerance (t/t) | 39.8 | 10.5 | 12 | 2.1 |
| Total tolerance (kmol/t) | 1973 | 863 | 951 | 369 |
| The power consumption of circulation gas (kwh/t) | 1550 | 340 | 200 | — |
| Freezing power consumption (kwh/t) | — | 450 | 275 | 220 |
| Total power consumption (kwh/t) | 1550 | 790 | 475 | 220 |
Can be drawn by the data in the above table 1, load volume, quenching tolerance and total tolerance and total electrisity consumption that the present invention produces trimeric cyanamide per ton are far smaller than common technology, and the consumption of its urea and fuel also less than common technology, has obvious improvement.
According to above embodiment, just can well realize the present invention.
Claims (10)
1. low pressure is produced the equipment of trimeric cyanamide, mainly is made up of the reactor drum, strainer, quencher, tripping device and the intermediates groove that connect in order, it is characterized in that, also is connected with exhaust fan, preheater, ammonia absorber on the said separator in order; The top of said ammonia absorber is connected with reactor drum with preheater through compressor, and said ammonia absorber top and ammonia compressor, ammonia cooler, ammonia storage tank and boosting pump are connected to form loop structure in order.
2. low pressure according to claim 1 is produced the equipment of trimeric cyanamide, it is characterized in that the top of said ammonia absorber is connected with quencher or said boosting pump is connected with quencher.
3. low pressure according to claim 2 is produced the equipment of trimeric cyanamide, it is characterized in that, said ammonia absorber bottom is connected to form loop structure in order with recycle pump and water cooler.
4. low pressure according to claim 3 is produced the equipment of trimeric cyanamide, it is characterized in that said tripping device is cyclonic separator or strainer.
5. the technology of utilizing each described equipment low pressure of claim 1～4 to produce trimeric cyanamide is characterized in that, mainly is made up of following steps:
(1) fusing urea gets into reactor drum after atomizing; As the reaction carrier gas, is that 380 ℃～410 ℃, pressure be deamination product that the condition of 0.1MPa～1.4MPa under reaction generate trimeric cyanamide, carbonic acid gas, ammonia and trimeric cyanamide at reactor temperature with gas ammonia;
(2) after reaction was accomplished, crystallization deamination product also filtered, and the gas after the filtration is processed finished product after cooling off, separate through quenching medium;
(3) remaining gas water absorbs back formation first ammonium solution and mixed gas after the above-mentioned separation;
(4) rectifying under-30 ℃～30 ℃ condition of above-mentioned mixed gas forms ammonia, and said ammonia returns step (1) do reaction carrier gas Huo ∕ and returns step (2) and make quenching medium.
6. low pressure according to claim 5 is produced the technology of trimeric cyanamide, it is characterized in that, the rectifying of above-mentioned mixed gas is to reduce the mixed gas method of temperature through the low temperature gas ammonia to realize.
7. according to the technology of claim 5 or 6 described low pressure production trimeric cyanamides, it is characterized in that the Tc of deamination product is 340 ℃～380 ℃ in the above-mentioned steps (2).
8. low pressure according to claim 7 is produced the technology of trimeric cyanamide, it is characterized in that, cooling temperature is 100 ℃～200 ℃ in the above-mentioned steps (2).
9. low pressure according to claim 8 is produced the technology of trimeric cyanamide, it is characterized in that filtering product in the above-mentioned steps (2) blows Returning reactor with hot ammonia.
10. low pressure according to claim 9 is produced the technology of trimeric cyanamide, it is characterized in that said quenching medium is an ammonia.
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| CN103601693A (en) * | 2013-10-23 | 2014-02-26 | 李东田 | One-step method used for production of melamine by circulating ammonia gas as carrying gas |
| CN103804311A (en) * | 2012-11-02 | 2014-05-21 | 华强化工集团股份有限公司 | Energy-saving melamine production process device |
| CN105218470A (en) * | 2015-08-22 | 2016-01-06 | 安徽金禾实业股份有限公司 | Solid and gas tripping device in a kind of Melamine Production |
| CN105829289A (en) * | 2013-12-17 | 2016-08-03 | 斯塔米卡邦有限公司 | Integrated production of urea and melamine |
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| CN105218470A (en) * | 2015-08-22 | 2016-01-06 | 安徽金禾实业股份有限公司 | Solid and gas tripping device in a kind of Melamine Production |
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Application publication date: 20120718 Assignee: Chengdu Ying Chemical Technology Co., Ltd. Assignor: Li Jingming|Liu Hongyu|Zhang Yu Contract record no.: 2017990000286 Denomination of invention: Equipment and process for producing melamine under low pressure Granted publication date: 20140827 License type: Exclusive License Record date: 20170718 |
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