CN102796055A - Optimum method for co-producing melamine and urea - Google Patents
Optimum method for co-producing melamine and urea Download PDFInfo
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- CN102796055A CN102796055A CN201210285822XA CN201210285822A CN102796055A CN 102796055 A CN102796055 A CN 102796055A CN 201210285822X A CN201210285822X A CN 201210285822XA CN 201210285822 A CN201210285822 A CN 201210285822A CN 102796055 A CN102796055 A CN 102796055A
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- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 title claims abstract description 96
- 239000004202 carbamide Substances 0.000 title claims abstract description 96
- 238000000034 method Methods 0.000 title claims abstract description 58
- 229920000877 Melamine resin Polymers 0.000 title claims abstract description 56
- JDSHMPZPIAZGSV-UHFFFAOYSA-N melamine Chemical compound NC1=NC(N)=NC(N)=N1 JDSHMPZPIAZGSV-UHFFFAOYSA-N 0.000 title claims abstract description 56
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 56
- 238000005516 engineering process Methods 0.000 claims abstract description 32
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 28
- 238000010791 quenching Methods 0.000 claims abstract description 26
- 230000000171 quenching effect Effects 0.000 claims abstract description 26
- 239000012071 phase Substances 0.000 claims abstract description 15
- 238000004519 manufacturing process Methods 0.000 claims abstract description 14
- 239000007790 solid phase Substances 0.000 claims abstract description 11
- 239000002994 raw material Substances 0.000 claims abstract description 6
- BAVYZALUXZFZLV-UHFFFAOYSA-N Methylamine Chemical compound NC BAVYZALUXZFZLV-UHFFFAOYSA-N 0.000 claims description 122
- 239000007789 gas Substances 0.000 claims description 85
- 239000007788 liquid Substances 0.000 claims description 74
- 230000008569 process Effects 0.000 claims description 30
- 238000009833 condensation Methods 0.000 claims description 25
- 230000005494 condensation Effects 0.000 claims description 25
- XZMCDFZZKTWFGF-UHFFFAOYSA-N Cyanamide Chemical compound NC#N XZMCDFZZKTWFGF-UHFFFAOYSA-N 0.000 claims description 24
- 210000000952 spleen Anatomy 0.000 claims description 24
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims description 20
- 239000002562 thickening agent Substances 0.000 claims description 18
- 239000000203 mixture Substances 0.000 claims description 15
- 238000005457 optimization Methods 0.000 claims description 15
- 239000006200 vaporizer Substances 0.000 claims description 15
- 238000013022 venting Methods 0.000 claims description 15
- 238000009472 formulation Methods 0.000 claims description 14
- 238000002360 preparation method Methods 0.000 claims description 13
- 210000002700 urine Anatomy 0.000 claims description 13
- 238000010521 absorption reaction Methods 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- 238000001704 evaporation Methods 0.000 claims description 7
- 230000008020 evaporation Effects 0.000 claims description 7
- 239000012808 vapor phase Substances 0.000 claims description 6
- 241000282326 Felis catus Species 0.000 claims description 5
- 239000012159 carrier gas Substances 0.000 claims description 4
- 230000015556 catabolic process Effects 0.000 claims description 4
- 238000006731 degradation reaction Methods 0.000 claims description 4
- 238000007701 flash-distillation Methods 0.000 claims description 4
- 238000003825 pressing Methods 0.000 claims description 4
- 238000004064 recycling Methods 0.000 claims description 4
- 239000006096 absorbing agent Substances 0.000 claims description 3
- 238000003795 desorption Methods 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 230000005611 electricity Effects 0.000 abstract description 3
- 230000000694 effects Effects 0.000 abstract description 2
- 230000015572 biosynthetic process Effects 0.000 abstract 1
- 238000000354 decomposition reaction Methods 0.000 abstract 1
- 238000004094 preconcentration Methods 0.000 abstract 1
- 238000003786 synthesis reaction Methods 0.000 abstract 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 5
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 2
- MKKVKFWHNPAATH-UHFFFAOYSA-N [C].N Chemical compound [C].N MKKVKFWHNPAATH-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 239000000618 nitrogen fertilizer Substances 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- PAWQVTBBRAZDMG-UHFFFAOYSA-N 2-(3-bromo-2-fluorophenyl)acetic acid Chemical compound OC(=O)CC1=CC=CC(Br)=C1F PAWQVTBBRAZDMG-UHFFFAOYSA-N 0.000 description 1
- JJEJDZONIFQNHG-UHFFFAOYSA-N [C+4].N Chemical compound [C+4].N JJEJDZONIFQNHG-UHFFFAOYSA-N 0.000 description 1
- 235000019270 ammonium chloride Nutrition 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000007907 direct compression Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to an optimum method for co-producing melamine and urea, the melamine production technology is characterized by comprising a gas phase quenching or solid phase quenching low pressure circulation method which takes urea as a raw material, an European science and technology high pressure method or a DSM low pressure method, and an urea device is a CO2 air stripping urea device. The optimum method has the following technical effects that the urea device enables matched reformation according to maximal coproduction melamine capability, and the productivity is increased by near 25% after merging with melamine tail gas, the capacity expansion reformation on synthesis ammonia is not required, because that a medium pressure decomposition system and an urea pre-concentration device are added, the vapor of urea per ton and unit consumption of electricity are not increased.
Description
Technical field
The present invention is adapted to Increasing Production and Energy Saving transformation and the ammonia of Melamine Production process discharge and the recycle of carbon dioxide tail gas or methylamine liquid coproduction urea of carbon dioxide stripping their urine device.
Technical background
With urea is a large amount of ammonia and the dioxide gass of trimeric cyanamide reaction process by-product of raw material; Need replenish the part ammonia because of process operation simultaneously; Need discharge 1.05 tons ammonia and 1.15 tons carbon dioxide gas mixture so produce 1 ton of trimeric cyanamide, be commonly called as tail gas; And ammonia and dioxide gas are the raw materials of urea production; So melamine and urea coproduction are best suited for from resource distribution; But different because of preparation technology of melamine, make melamine tail gas coproduction urea that very big difference arranged on energy consumption and operation stability.High-pressure process melamine tail gas for Europe skill company gets into urea plant with middle pressure methylamine liquid; Need carry out desorb to the low pressure methylamine liquid that melamine tail gas produces for the low-pressure process of DSM carries dense; Get into urea plant after becoming pressure methylamine liquid, although it is two kinds of technologies are the lower middle pressure methylamine liquid of water cut, bigger to the steam/hydrocarbons ratio influence of urea system; Need very big urea plant supporting on the one hand for certain trimeric cyanamide device, the urea steam mono-consumption of urea plant increases on the other hand.It is exactly the normal pressure gas phase quenching of BASF and the improvement pressurization gas phase quenching technology of China that another of Melamine Production represented technology; The great advantage of this technology is no steam consumption; Technical process weak point, less investment, energy consumption are low; Especially the power consumption of the improvement pressurization gas phase quenching technology of China has descended approximately 50% than the normal pressure gas phase quenching technology of BASF, and single cover throughput can reach more than 60,000 tons, and power consumption drops to below 800 degree.Although improvement gas phase quenching technology tail gas pressure is brought up to more than the 0.3MPa (A); If can reach more than the 0.6MPa (A) from the discharge of carrier gas compressor outlet branch; But make the tail gas of large-scale trimeric cyanamide device incorporate urea plant into; Tail gas is compressed to press absorbs in carrying out more than the 1.8MPa, or carry out middle pressure desorb more than the 1.8MPa after tail gas low pressure absorbed again and carry densely, or carry out ammonia carbon and separate; The dense 2.0MPa steam of ton melamine tail gas needs more than 4 tons that separates with ammonia carbon is carried in desorb; So high steam consumption has seriously restricted the development of this operational path; Though directly compression is significantly less than the low pressure absorption to tail gas on energy consumption, middle pressure is resolved technology; But, be bonded in easily on the impeller of turbocompressor because the volumetric flow rate of tail-gas compressor is little, runner is narrow, has difficult isolating sticky contaminant in the melamine tail gas; Had a strong impact on the long-period stable operation of melamine tail gas compressor; So trimeric cyanamide gas phase quenching technology does not obtain the perfect unity of less energy-consumption and long-term operation on tail gas coproduction urea technique, the compelled products such as the low carbon ammonium that is unfavorable for long-distance transportation again of some fertilizer efficiency, ammonium chloride, ammonium nitrate of producing, producing 1 ton of trimeric cyanamide need 3 tons of urea; Be equivalent to have 1.5 tons of urea to become poor efficiency nitrogenous fertilizer, increased traffic capacity by high-efficiency nitrogen fertilizer.
Summary of the invention
Technical problem to be solved by this invention provides that a kind of comprehensive energy consumption is low, the trimeric cyanamide and the urea co-production of less investment, stable suitable low-pressure vapor phase quenching, Europe skill high-pressure process or DSM low-pressure process.
Adopt following technical scheme in order to solve the problems of the technologies described above: the method for a kind of trimeric cyanamide of optimization and urea coproduction; Described preparation technology of melamine is meant with urea to be gas phase quenching or solid phase quenching low pressure recycle method technology, Europe skill high-pressure process or the DSM low-pressure process of raw material, and said urea plant is meant CO
2Gas formulation urea plant.
Low-pressure vapor phase or solid phase quenching melamine tail gas that pressure 0.4MPa is above, the co-production of the low pressure condensation absorber portion of urea plant is directly sent in branch's discharge before the carrier gas recycle compressor.
Europe skill high-pressure process or DSM low-pressure process melamine tail gas absorption liquid are directly sent into the one section vaporizer of urea plant or the co-production of urine preconcentrator.
Described absorption liquid is a first ammonium liquid.
Described CO
2In the gas formulation urea plant, between high pressure section and low-pressure stage, increased the middle pressure flash distillation thermal degradation section of pressure 1.8 ~ 2.2 MPa (A).
Described CO
2In the gas formulation urea plant; Gas phase or solid phase quenching melamine tail gas condensed and absorbed operating unit have been increased; The low pressure branch is vented one's spleen and is become low pressure methylamine liquid I with the exhaust gas mixing condensation of urea plant desorption tower; Melamine tail gas and low pressure methylamine liquid I are mixed into melamine tail gas condensed and absorbed operating unit, and the methylamine liquid after the absorption melamine tail gas is low pressure methylamine liquid II, and methylamine liquid II is sent into urine preconcentrator and one section vaporizer through middle pressure metro-methylamine pump.
Described CO
2In the gas formulation urea plant, after low pressure is decomposed section, increased the urine preconcentrator, pressed in being used for recycling and divide the heat of condensation of venting one's spleen.
Preparation technology of melamine adopts gas phase quenching or solid phase quenching low pressure recycle method technology; In press to divide to vent one's spleen and send into one section vaporizer shell side with part low pressure methylamine liquid II is mixed; The shell side condensing temperature is 135 ℃, one section first ammonium liquid and uncooled NH that the vaporizer shell side comes out
3, CO
2With water vapour and the mixed shell side that gets into the prevapourising thickener of remaining low pressure methylamine liquid II; The shell side condensing temperature is 120 ℃; Walk urea soln in prevapourising thickener and one section evaporator tube; Press to divide the heat of condensation evaporation concentration urea soln to 130 of venting one's spleen ℃ in the utilization, concentration reaches 95 ~ 96%, and the methylamine liquid that prevapourising thickener shell side comes out is pressed the methylamine thermosistor in flowing into.
Preparation technology of melamine adopts Europe skill high-pressure process or DSM low-pressure process; The methylamine liquid of the tail gas of preparation technology of melamine is directly vented one's spleen with the middle pressure branch of urea plant through a middle pressure metro-methylamine pump part and is mixed the shell side of sending into one section vaporizer; The shell side condensing temperature is 135 ℃, one section first ammonium liquid and uncooled NH that the vaporizer shell side comes out
3, CO
2With the mixed shell side that gets into the prevapourising thickener of the low pressure first ammonium liquid of water vapour and remaining triamine tail gas first ammonium liquid and urea system self; The shell side condensing temperature is 120 ℃; Walk urea soln in prevapourising thickener and one section evaporator tube, press to divide the heat of condensation evaporation concentration urea soln to 130 of venting one's spleen ℃ in the utilization, concentration reaches 95 ~ 96%; Press in making and divide the heat of condensation of venting one's spleen to obtain utilizing, the methylamine liquid that prevapourising thickener shell side comes out is pressed the methylamine thermosistor in flowing into.
Described CO
2In the gas formulation urea plant; In order to increase the receptivity of melamine tail gas as far as possible, increase superfluous ammonia separating rectification tower, the tower top outlet temperature is controlled at 10 ~ 40 ℃; Tower top pressure 0.3 ~ 0.4MPa (A); From the superfluous ammonia of part that cat head is discharged, behind compressor compresses to 1.8 ~ 2.2 MPa (A), press the methylamine thermosistor in sending into after pressing methylamine liquid thermosistor condensation in sending into or directly being condensed into liquefied ammonia; To press the ctystallizing point of first ammonium liquid in reducing, the first ammonium liquid that the methylamine thermosistor comes out is sent into high pressure scrubber or high pressure methylamine condensing surface through the high pressure metro-methylamine pump.
The present invention has following technique effect: 1, urea plant is by the supporting transformation of maximum combined production of melamine ability, and incorporating after the melamine tail gas urea plant production capacity into increases closely 25%, but need not carry out capacity expansion revamping to synthetic ammonia; 2, for low-pressure vapor phase quenching technology, although urea plant is incorporated into after the melamine tail gas because the increase of output causes CO
2The gas stripping efficiency of gas stripping column, the CO of synthetic tower
2Transformation efficiency reduces, but owing to increased middle pressure decomposing system and urine preconcentrator, the steam of ton urea and the unit consumption of electricity is not increased; 3, for low-pressure vapor phase quenching technology, improved co-generation system has been avoided the direct compression of melamine tail gas, has guaranteed the long-period stable operation of co-generation system; 4, for Europe skill high-pressure process, DSM low-pressure process melamine processes, after urea plant is incorporated the melamine tail gas absorption liquid into, although because the increase of output causes CO
2The gas stripping efficiency of gas stripping column, the CO of synthetic tower
2Transformation efficiency reduces, but owing to increased middle pressure decomposing system and urine preconcentrator, the steam of ton urea and the unit consumption of electricity is not increased; 5, for Europe skill high-pressure process, DSM low-pressure process melamine processes; After urea plant is incorporated the melamine tail gas absorption liquid into; Although brought extraneous water,, make to get into the NH that low pressure absorbs methylamine liquid owing to increased middle pressure decomposing system and superfluous ammonia rectifying separation tower to urea system
3And CO
2Amount significantly reduces, and through reducing ammonia still process tower top outlet temperature, can effectively control low pressure and absorb the H that contains in the methylamine liquid
2The O amount, thus the steam/hydrocarbons ratio of synthetic tower import is effectively controlled.
Description of drawings
Fig. 1 is the process flow diagram of the embodiment of the invention 2.
Fig. 2 is the process flow diagram of the embodiment of the invention 3.
Embodiment
Embodiment 1: the method for a kind of trimeric cyanamide of optimization and urea coproduction, described preparation technology of melamine are meant with urea to be the gas phase quenching low pressure recycle method technology of raw material, and said urea plant is meant CO
2Gas formulation urea plant.
CO of the present invention
2Gas formulation urea plant and conventional CO
2The vaporizing extract process urea plant is compared: press flash distillation thermal degradation operating unit in a, the increase, preferred 1.8 ~ 2.2 MPa of pressure (A).
B, increase urine preconcentrator are pressed in the recycling and are decomposed the gas heat of condensation.
C, increase superfluous ammonia separating rectification tower operating unit, be used for separating the pressure of the superfluous ammonia of low pressure branch in venting one's spleen with control urea low pressure decomposing system, superfluous ammonia separates from cat head discharges, and the first ammonium liquid that superfluous ammonia separating rectification tower tower still is discharged is low pressure methylamine liquid I.
D, the superfluous ammonia compressed element of increase, pressure methylamine liquid thermosistor in sending into after pressing methylamine liquid thermosistor condensation or directly be condensed into liquefied ammonia during the superfluous ammonia that discharge on superfluous ammonia separating rectification tower top being sent into behind compressor compresses to 1.8 ~ 2.2 MPa (A).
Methylamine liquid after e, the process temperature adjustment is sent into high pressure scrubber and high pressure methylamine condensing surface with the high pressure metro-methylamine pump.
Embodiment 2: as shown in Figure 1; The method of a kind of trimeric cyanamide of optimization and urea coproduction; Preparation technology of melamine adopts pressure 0.4MPa above low-pressure vapor phase or solid phase quenching melamine tail gas; Branch discharges before the carrier gas recycle compressor, directly sends into the co-production of the low pressure condensation absorber portion of urea plant.
CO
2In the gas formulation urea plant, between high pressure section and low-pressure stage, increased the middle pressure flash distillation thermal degradation section of pressure 1.8 ~ 2.2 MPa (A).Gas phase or solid phase quenching melamine tail gas condensed and absorbed operating unit have been increased; The low pressure branch is vented one's spleen and is become low pressure methylamine liquid I with the exhaust gas mixing condensation of urea plant desorption tower; Melamine tail gas and low pressure methylamine liquid I are mixed into melamine tail gas condensed and absorbed operating unit; Methylamine liquid after the absorption melamine tail gas is low pressure methylamine liquid II, and methylamine liquid II is sent into urine preconcentrator and one section vaporizer through middle pressure metro-methylamine pump.Middle pressure branch is vented one's spleen and is sent into the shell side of one section evaporation with part methylamine liquid II, one section first ammonium liquid and uncooled NH that the vaporizer shell side comes out
3, CO
2With water vapour and the mixed shell side that gets into the prevapourising thickener of remaining low pressure methylamine liquid II; The shell side condensing temperature is 120 ℃; Walk urea soln in prevapourising thickener and one section evaporator tube, press to divide the heat of condensation evaporation concentration urea soln to 130 of venting one's spleen ℃ in the utilization, concentration reaches 95 ~ 96%; Press in making and divide the heat of condensation of venting one's spleen to obtain utilizing, the methylamine liquid that prevapourising thickener shell side comes out is pressed the methylamine thermosistor in flowing into.In order to increase the receptivity of melamine tail gas as far as possible; Increase superfluous ammonia separating rectification tower; The tower top outlet temperature is controlled at 10 ~ 40 ℃, and tower top pressure 0.3 ~ 0.4MPa (A) is from the superfluous ammonia of the part of cat head discharge; Behind compressor compresses to 1.8 ~ 2.2 MPa (A); Press the methylamine thermosistor in sending into after sending into pressure methylamine liquid thermosistor condensation or directly being condensed into liquefied ammonia, to press the ctystallizing point of first ammonium liquid in reducing, the first ammonium liquid that the methylamine thermosistor comes out is sent into high pressure scrubber through the high pressure metro-methylamine pump.The superfluous ammonia amount size of extracting out from cat head is that the size according to supporting trimeric cyanamide output decides, if supporting trimeric cyanamide ability is less, just can separate superfluous ammonia.
Other are with embodiment 1.
Embodiment 3: as shown in Figure 2; The method of a kind of trimeric cyanamide of optimization and urea coproduction, preparation technology of melamine adopt Europe skill high-pressure process or DSM low-pressure process melamine tail gas absorption liquid directly to send into the urine preconcentrator of urea plant and the co-production of one section vaporizer.Described absorption liquid is a first ammonium liquid.
CO
2In the gas formulation urea plant, after low pressure is decomposed section, increased the urine preconcentrator, pressed in being used for recycling and divide the heat of condensation of venting one's spleen.The methylamine liquid of the tail gas of preparation technology of melamine is directly vented one's spleen with the middle pressure branch of urea plant through a middle pressure metro-methylamine pump part and is mixed the shell side of sending into one section vaporizer, and the shell side condensing temperature is 135 ℃, one section first ammonium liquid and uncooled NH that the vaporizer shell side comes out
3, CO
2With the mixed shell side that gets into the prevapourising thickener of the low pressure methylamine liquid of water vapour and remaining triamine tail gas first ammonium liquid and urea system self; The shell side condensing temperature is 120 ℃; Walk urea soln in prevapourising thickener and one section evaporator tube, press to divide the heat of condensation evaporation concentration urea soln to 130 of venting one's spleen ℃ in the utilization, concentration reaches 95 ~ 96%; Press in making and divide the heat of condensation of venting one's spleen to obtain utilizing, the methylamine liquid that prevapourising thickener shell side comes out is pressed the methylamine thermosistor in flowing into.
Other are with embodiment 1.
Claims (10)
1. the method for the trimeric cyanamide of an optimization and urea coproduction; It is characterized in that: described preparation technology of melamine is meant with urea to be gas phase quenching or solid phase quenching low pressure recycle method technology, Europe skill high-pressure process or the DSM low-pressure process of raw material, and said urea plant is meant CO
2Gas formulation urea plant.
2. the method for the trimeric cyanamide of a kind of optimization according to claim 1 and urea coproduction; It is characterized in that: low-pressure vapor phase or solid phase quenching melamine tail gas that pressure 0.4MPa is above; Branch discharges before the carrier gas recycle compressor, directly sends into the co-production of the low pressure condensation absorber portion of urea plant.
3. the method for the trimeric cyanamide of a kind of optimization according to claim 1 and urea coproduction, it is characterized in that: Europe skill high-pressure process or DSM low-pressure process melamine tail gas absorption liquid are directly sent into the co-production of the urine preconcentrator of urea plant.
4. the method for the trimeric cyanamide of a kind of optimization according to claim 3 and urea coproduction, it is characterized in that: described absorption liquid is a first ammonium liquid.
5. according to the trimeric cyanamide of claim 2 or 3 described a kind of optimizations and the method for urea coproduction, it is characterized in that: described CO
2In the gas formulation urea plant, between high pressure section and low-pressure stage, increased the middle pressure flash distillation thermal degradation section of pressure 1.8 ~ 2.2 MPa (A).
6. the method for the trimeric cyanamide of a kind of optimization according to claim 2 and urea coproduction is characterized in that: described CO
2In the gas formulation urea plant; Gas phase or solid phase quenching melamine tail gas condensed and absorbed operating unit have been increased; The low pressure branch is vented one's spleen and is become low pressure methylamine liquid I with the desorption tower exhaust gas mixing condensation of urea plant; Melamine tail gas and low pressure methylamine liquid I are mixed into melamine tail gas condensed and absorbed operating unit, and the methylamine liquid after the absorption melamine tail gas is low pressure methylamine liquid II, and methylamine liquid II is sent into the urine preconcentrator through middle pressure metro-methylamine pump.
7. according to the trimeric cyanamide of claim 2 or 3 described a kind of optimizations and the method for urea coproduction, it is characterized in that: described CO
2In the gas formulation urea plant, after low pressure is decomposed section, increased the urine preconcentrator, pressed in being used for recycling and divide the heat of condensation of venting one's spleen.
8. the method for the trimeric cyanamide of a kind of optimization according to claim 2 and urea coproduction; It is characterized in that: preparation technology of melamine adopts gas phase quenching or solid phase quenching low pressure recycle method technology; The middle branch of pressing is vented one's spleen and the mixed shell side of sending into one section vaporizer of part low pressure methylamine liquid II; The shell side condensing temperature is 135 ℃, one section first ammonium liquid and uncooled NH that the vaporizer shell side comes out
3, CO
2With water vapour and the mixed shell side that gets into the prevapourising thickener of remaining low pressure methylamine liquid II; The shell side condensing temperature is 120 ℃; Walk urea soln in prevapourising thickener and one section evaporator tube, press to divide the heat of condensation evaporation concentration urea soln to 130 of venting one's spleen ℃ in the utilization, concentration reaches 95 ~ 96%; Press in making and divide the heat of condensation of venting one's spleen to obtain utilizing, the methylamine liquid that prevapourising thickener shell side comes out is pressed the methylamine thermosistor in flowing into.
9. the method for the trimeric cyanamide of a kind of optimization according to claim 3 and urea coproduction; It is characterized in that: preparation technology of melamine adopts Europe skill high-pressure process or DSM low-pressure process; The tail gas methylamine liquid of preparation technology of melamine is vented one's spleen with the middle pressure branch of urea plant through a middle pressure metro-methylamine pump part and is mixed the shell side of sending into one section vaporizer; The shell side condensing temperature is 135 ℃, one section first ammonium liquid and uncooled NH that the vaporizer shell side comes out
3, CO
2With the mixed shell side that gets into the prevapourising thickener of the low pressure methylamine liquid of water vapour and remaining triamine tail gas first ammonium liquid and urea system self; The shell side condensing temperature is 120 ℃; Walk urea soln in prevapourising thickener and one section evaporator tube, press to divide the heat of condensation evaporation concentration urea soln to 130 of venting one's spleen ℃ in the utilization, concentration reaches 95 ~ 96%; Press in making and divide the heat of condensation of venting one's spleen to obtain utilizing, the methylamine liquid that prevapourising thickener shell side comes out is pressed the methylamine thermosistor in flowing into.
10. according to the trimeric cyanamide of claim 2 or 3 described a kind of optimizations and the method for urea coproduction, it is characterized in that: described CO
2In the gas formulation urea plant; In order to increase the receptivity of melamine tail gas as far as possible, increase superfluous ammonia separating rectification tower, the tower top outlet temperature is controlled at 10 ~ 40 ℃; Tower top pressure 0.3 ~ 0.4MPa (A); From the superfluous ammonia of part that cat head is discharged, behind compressor compresses to 1.8 ~ 2.2 MPa (A), press the methylamine thermosistor in sending into after pressing methylamine liquid thermosistor condensation in sending into or directly being condensed into liquefied ammonia; To press the ctystallizing point of first ammonium liquid in reducing, the first ammonium liquid that the methylamine thermosistor comes out is sent into high pressure scrubber or high pressure methylamine condensing surface through the high pressure metro-methylamine pump.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103145635A (en) * | 2013-03-05 | 2013-06-12 | 中国五环工程有限公司 | Tail gas recycling process and system for melamine production device |
| CN106167470A (en) * | 2016-07-26 | 2016-11-30 | 湖北宜化集团有限责任公司 | A kind of tripolycyanamide of holding successfully reclaims the system and method for urea plant |
| CN110041230A (en) * | 2019-04-30 | 2019-07-23 | 中国五环工程有限公司 | Recycle the vaporizing extract process urea production process of melamine plant tail gas |
| CN111635338A (en) * | 2020-06-09 | 2020-09-08 | 兖矿集团有限公司 | Device for co-production of carbon dioxide gas stripping urea device and high-pressure method melamine device and production method |
| CN115745845A (en) * | 2022-11-04 | 2023-03-07 | 重庆建峰化工股份有限公司 | Urea and urea production system for absorbing melamine tail gas |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103145635A (en) * | 2013-03-05 | 2013-06-12 | 中国五环工程有限公司 | Tail gas recycling process and system for melamine production device |
| CN103145635B (en) * | 2013-03-05 | 2014-12-03 | 中国五环工程有限公司 | Tail gas recycling process and system for melamine production device |
| CN106167470A (en) * | 2016-07-26 | 2016-11-30 | 湖北宜化集团有限责任公司 | A kind of tripolycyanamide of holding successfully reclaims the system and method for urea plant |
| CN110041230A (en) * | 2019-04-30 | 2019-07-23 | 中国五环工程有限公司 | Recycle the vaporizing extract process urea production process of melamine plant tail gas |
| CN110041230B (en) * | 2019-04-30 | 2021-10-15 | 中国五环工程有限公司 | Process for producing urea by stripping method for recovering tail gas of melamine device |
| CN111635338A (en) * | 2020-06-09 | 2020-09-08 | 兖矿集团有限公司 | Device for co-production of carbon dioxide gas stripping urea device and high-pressure method melamine device and production method |
| CN115745845A (en) * | 2022-11-04 | 2023-03-07 | 重庆建峰化工股份有限公司 | Urea and urea production system for absorbing melamine tail gas |
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