CN1279000C - Production process of high-nitrogen large-grain urea - Google Patents
Production process of high-nitrogen large-grain urea Download PDFInfo
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- CN1279000C CN1279000C CN 200410090876 CN200410090876A CN1279000C CN 1279000 C CN1279000 C CN 1279000C CN 200410090876 CN200410090876 CN 200410090876 CN 200410090876 A CN200410090876 A CN 200410090876A CN 1279000 C CN1279000 C CN 1279000C
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- urea
- nitrogen
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- grains
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- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 title claims abstract description 129
- 239000004202 carbamide Substances 0.000 title claims abstract description 69
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 26
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 19
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 14
- 239000000428 dust Substances 0.000 claims abstract description 15
- 238000005516 engineering process Methods 0.000 claims abstract description 14
- 238000005469 granulation Methods 0.000 claims abstract description 14
- 230000003179 granulation Effects 0.000 claims abstract description 14
- LEQAOMBKQFMDFZ-UHFFFAOYSA-N glyoxal Chemical compound O=CC=O LEQAOMBKQFMDFZ-UHFFFAOYSA-N 0.000 claims abstract description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 11
- 229940015043 glyoxal Drugs 0.000 claims abstract description 6
- 235000013877 carbamide Nutrition 0.000 claims description 62
- 238000005406 washing Methods 0.000 claims description 12
- 239000007921 spray Substances 0.000 claims description 7
- 238000009477 fluid bed granulation Methods 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 3
- 238000012856 packing Methods 0.000 claims description 2
- 238000005054 agglomeration Methods 0.000 abstract 1
- 230000002776 aggregation Effects 0.000 abstract 1
- 238000000889 atomisation Methods 0.000 abstract 1
- 239000012467 final product Substances 0.000 abstract 1
- 239000000203 mixture Substances 0.000 abstract 1
- 239000000843 powder Substances 0.000 abstract 1
- 239000000047 product Substances 0.000 abstract 1
- 238000010298 pulverizing process Methods 0.000 abstract 1
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 15
- 239000007789 gas Substances 0.000 description 10
- 238000000034 method Methods 0.000 description 9
- 239000000243 solution Substances 0.000 description 8
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- ZNZYKNKBJPZETN-WELNAUFTSA-N Dialdehyde 11678 Chemical compound N1C2=CC=CC=C2C2=C1[C@H](C[C@H](/C(=C/O)C(=O)OC)[C@@H](C=C)C=O)NCC2 ZNZYKNKBJPZETN-WELNAUFTSA-N 0.000 description 5
- 238000005496 tempering Methods 0.000 description 5
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 239000003337 fertilizer Substances 0.000 description 3
- 238000005243 fluidization Methods 0.000 description 3
- 239000008098 formaldehyde solution Substances 0.000 description 3
- ZZUFCTLCJUWOSV-UHFFFAOYSA-N furosemide Chemical compound C1=C(Cl)C(S(=O)(=O)N)=CC(C(O)=O)=C1NCC1=CC=CO1 ZZUFCTLCJUWOSV-UHFFFAOYSA-N 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000000654 additive Substances 0.000 description 2
- 230000000996 additive effect Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- OHJMTUPIZMNBFR-UHFFFAOYSA-N biuret Chemical compound NC(=O)NC(N)=O OHJMTUPIZMNBFR-UHFFFAOYSA-N 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 235000019628 coolness Nutrition 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 125000001145 hydrido group Chemical group *[H] 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000005200 wet scrubbing Methods 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- WSFSSNUMVMOOMR-NJFSPNSNSA-N methanone Chemical compound O=[14CH2] WSFSSNUMVMOOMR-NJFSPNSNSA-N 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- 230000000050 nutritive effect Effects 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- -1 urea aldehyde Chemical class 0.000 description 1
- 150000003672 ureas Chemical class 0.000 description 1
- 239000006200 vaporizer Substances 0.000 description 1
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Abstract
The present invention discloses production technology for large high-nitrogen urea grains (the grain diameter is from 2 to 8MM). When large high-nitrogen grains are produced, 90% to 99% of urea solution and glyoxal solution are granulated by granulation technology by an atomization fluidized bed after mixed according to the weight ratio of 100: 0.05 to 0.25; the mixture is prepared into the large urea grains after cooled; air containing urea powder dust is discharged by a granulator and a final product cooler and sprayed to be washed by water at the normal temperature and the normal pressure. The nitrogen content of the large high-nitrogen grain urea obtained by the present invention can reach 46.4% to reach the national standard GB2440-2001 of superior products. The large high-nitrogen grain urea obtained by the present invention has the advantages of large grains, uniform grains, high intensity, good flowability, difficult pulverization, no agglomeration and convenient storage and use.
Description
Technical field
The present invention relates to a kind of urea production process, specifically, be a kind of be the production process of high-nitrogen large-grain urea of additive with oxalic dialdehyde.
Background technology
At present, by ammonia and CO
2Synthetic prepared solid urea is a kind of most important nitrogen fertilizers, and it is widely used in agriculture production and uses as fertilizer.
The processing method of producing granular urea mainly contains: Hydro (HYDRO) and Toyo Engineering Corporation (TEC) fluidized bed granulation process.The former is the atomizing fluidized-bed, and the latter all adds the urea aldehyde cpd that the reaction of a small amount of additive formaldehyde solution or formaldehyde and urea soln is produced for spraying fluidized-bed in granulation process.
Hydro company granular urea production technique is seen Fig. 2: the urea soln of raw material 95% (wt) concentration is delivered to tablets press 22 through granulation feeding pump 21 and is carried out granulation.In urea soln transfer lime 23, add the formaldehyde (with the formaldehyde solution of 37% concentration) that accounts for product volume 0.4～0.5% (wt) through line mixer 24.Tablets press is a fluidized bed prilling equipment, comprises fluidization air blower fan 25 and atomizing air blower fan 26 and urea soln atomizing nozzle 27.The granular urea that tablets press is made is through bucket elevator 28, and urea sieve 29 sieves out the granular urea product of granularity φ 2～4mm or φ 5～8mm, becomes qualified granular urea product after product cooler 30 coolings.In addition, from the air admission dust washing tower 31 that contains carbamide dust of tablets press and reactor product cooler discharge, after the water wet scrubbing, tail gas enters atmosphere.Contain carbamide dust 30mg/m in the general tail gas
3, contain ammonia 300～500mg/m
3
Toyo Engineering Corporation's granular urea production technique is seen Fig. 3: the urea soln of raw material 95～98% (wt) concentration is delivered to tablets press 42 through granulation feeding pump 41 and is carried out granulation.Wherein seldom a part of urea soln is delivered in the MMU reactor 43 and is reacted formation MMU solution with the formaldehyde solution of 37% concentration.This solution is delivered in the granulation feeding pump outlet line 46 one and is gone forward side by side in the tablets press by MMU feeding pump 45 after vaporizer 44 further concentrates.Granulating system comprises: injection nozzle 47, fluidization air blower fan 48 and injection air blower fan 49 etc.The granular urea that tablets press is made is through bucket elevator 50, and urea sieve 51 sieves out the granular urea product of granularity φ 2～4mm or φ 5～8mm, becomes qualified granular urea product after product cooler 52 coolings.In addition, from the air admission dust washing tower 53 that contains carbamide dust of tablets press and reactor product cooler discharge, after the water wet scrubbing, tail gas enters atmosphere.Contain carbamide dust 30mg/m as one u in the tail gas
3, contain ammonia 300～500mg/m
3
The urea product that above-mentioned two kinds of technologies are produced does not contain the required nutritive ingredient of other crop except that containing the single nitrogen fertilizers of urea.Facts have proved that this urea product nitrogen content is more than 46% (wt), and the crop absorption utilization ratio is generally about 35% (wt), unabsorbed nitrogen is lost in the soil, causes the secondary pollution of rivers and lakes water system.This also is the major cause of present domestic rivers and lakes water system eutrophication.In addition, still contain a large amount of free ammonias in the discharging tail gas, environment is polluted.
Summary of the invention
The purpose of this invention is to provide a kind of GB2440-2001 that can be up to state standards and to satisfy the needs of farm crop again, can overcome the novel process of the above-mentioned two kinds of insufficient production high-nitrogen large-grain of technology urea simultaneously again nutrient.
For achieving the above object, the present invention takes following steps:
A. with the urea soln of 90%-99% (wt) and glyoxal solution by weight 100: 0.05-0.25, at pressure is that 0.1-0.2MPa and temperature are 130-135 ℃ of mixing down, after carrying out granulation with atomizing fluid bed granulation technology again, through bucket elevator carry and urea sieve sieve out the product of granularity Φ 2-4mm or Φ 5-8mm after, be cooled to below 50 ℃ through product cooler again and obtain granular urea.
B. the air that contains carbamide dust of tablets press and product cooler discharge adopts water to carry out spray washing under normal temperature and normal pressure.
In the described steps A, during the atomizing fluid bed granulation, the tablets press fluidized-bed temperature is 115 ℃, and the exported product temperature is 90 ℃.
Among the described step B, during spray washing, washing tower is packing tower, sieve-tray tower or spray column.
Adopt the described weight ratio of steps A can not produce wearing and tearing to granulation feeding pump and granulation nozzle through mixing.
Characteristics such as atomizing fluid bed granulation technology is adopted in granulation, and material is a stainless steel, has big, the difficult obstruction of throughput, anticorrosive, and is high temperature resistant.
The tail gas that tablets press and reactor product cooler are discharged contains the carbamide dust amount in the discharging tail gas and reduces to 20mg/M after water washing
3Below, nitrogen content increases to 46.4% (wt) by 46.2% of above-mentioned two kinds of technologies, reaches national up-to-date urea top grade product standard GB2440-2001.
Solution of the present invention except that other has specified otherwise, all refers to the aqueous solution.
The high-nitrogen large-grain urea product has following principal feature:
(1) the nitrogenous height of product;
(2) adding the oxalic dialdehyde amount is the 0.05%-0.25% (wt) of urea amount, only for above-mentioned two kinds of technology formaldehyde add-ons about 1/5 (above-mentioned two technologies all add about 0.5% (wt) of formaldehyde, thereby have reduced the urea cost.Simultaneously, alleviate the load of urea evaporator section, reduced energy consumption about 1%;
(3) product has the effect of slow release long-acting owing to add the comparatively strong compound action of oxalic dialdehyde, impels the effective rate of utilization of nitrogen to improve more than 10%.
This technology makes granular urea product component, granularity and crushing force with above-mentioned two kinds of technologies and is compared as follows:
The granular urea product that Hydro and Toyo Engineering Corporation produce:
Urea 98.45% (wt)
Biuret (increasing amount) 0.1% (wt)
Formaldehyde 0.5% (wt)
Water 0.3% (wt)
Distribution of particle sizes Φ 2～4mm 〉=90% or Φ 4～8mm 〉=90%
Crushing force Φ 3.2mm 30N minimum
Φ 6.2mm 100N minimum
The compound sulfenyl granular urea product of this explained hereafter:
Urea 98.55%-98.85% (wt)
Biuret (increasing amount) 0.1% (wt)
Oxalic dialdehyde 0.1% (wt)
Water 0.3% (wt)
Distribution of particle sizes Φ 2～4mm 〉=92% or Φ 4～8mm 〉=92%
Crushing force Φ 3.2mm 33N minimum
Φ 6.2mm 110N minimum
Description of drawings
Fig. 1 is a process flow diagram of the present invention.
Fig. 2 is a Hydro company granular urea technological process of production synoptic diagram in the prior art.
Fig. 3 is Toyo Engineering Corporation's granular urea technological process of production synoptic diagram in the prior art.
Embodiment
Be described in detail content of the present invention below with reference to Fig. 1.
Raw material is the urea soln of 98% (wt) for the concentration that makes from the urea synthesis decomposition process, enters tempering tank 3 after pipeline 1 and under meter 2 meterings.
In addition, glyoxal solution is sent into tempering tank through glyoxal solution groove 6, oxalic dialdehyde volume pump 7.At pressure is that 0.15MPa, temperature are to mix under 132 ℃ the condition.After above-mentioned two kinds of materials stir in tempering tank, deliver to by urea soln feeding pump 19 and to carry out granulation in the tablets press 10.The part by weight of urea soln and glyoxal solution is respectively 100 kilograms and 0.1 kilogram in tempering tank.
Granulating system is made up of atomizing fluidized bed pelletizer, fluidization air blower fan 12, atomizing air blower fan 13 and atomizing nozzle 11 etc.The tablets press fluidized-bed temperature is 115 ℃, and the exported product temperature is 90 ℃.The granular urea product of being made by tablets press sieves out the granular urea product of granularity Φ 2-4mm through bucket elevator 14, urea sieve 15, obtains qualified product after product cooler 16 is cooled to 50 ℃.
The air that contains carbamide dust from tablets press and product cooler discharge enters dust washing tower 17, and water washs.This dust washing tower 17 is a spray column.Circulating cleaning solution is sent in the tempering tank through circulate soln pump 18 and is recycled.Washing back tail gas enters atmosphere, contains Dust Capacity 20mg/M in the tail gas
3, other technologies have reduced the quantity discharged of the dust in the discharging gas relatively, better satisfy environmental protection requirement, significantly reduce atmospheric pollution.
Claims (3)
1. a production process of high-nitrogen large-grain urea is characterized in that, adopts following steps:
A. with the urea soln of 90-99wt% and glyoxal solution by weight 100: 0.05-0.25, at pressure is that 0.1-0.2MPa and temperature are 130-135 ℃ of mixing down, again after atomizing fluid bed granulation technology is carried out granulation, through bucket elevator carry and urea sieve sieve out the product of granularity Φ 2-4mm or Φ 5-8mm after, be cooled to below 50 ℃ through product cooler again and obtain granular urea;
B. the air that contains carbamide dust of tablets press and product cooler discharge adopts water to carry out spray washing under normal temperature and normal pressure.
2. production process of high-nitrogen large-grain urea according to claim 1 is characterized in that: in the described steps A, and during the atomizing fluid bed granulation, 115 ℃ of tablets press fluidized-bed temperatures, 90 ℃ of exported product temperature.
3. production process of high-nitrogen large-grain urea according to claim 1 is characterized in that: among the described step B, during spray washing, washing tower is packing tower, sieve-tray tower or spray column.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410090876 CN1279000C (en) | 2004-11-16 | 2004-11-16 | Production process of high-nitrogen large-grain urea |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410090876 CN1279000C (en) | 2004-11-16 | 2004-11-16 | Production process of high-nitrogen large-grain urea |
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| Publication Number | Publication Date |
|---|---|
| CN1706777A CN1706777A (en) | 2005-12-14 |
| CN1279000C true CN1279000C (en) | 2006-10-11 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200410090876 Expired - Fee Related CN1279000C (en) | 2004-11-16 | 2004-11-16 | Production process of high-nitrogen large-grain urea |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102014108703A1 (en) * | 2014-06-20 | 2015-12-24 | Thyssenkrupp Ag | Urea composition and process for its preparation |
| CN106984243B (en) * | 2016-12-27 | 2021-07-16 | 绿色造粒有限公司 | Urea granulation process without adding formaldehyde |
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Owner name: BEIJING FENGHAN ENGINEERING CONSULTATIVE CO., LTD Free format text: FORMER OWNER: WANG WEI; XU YAOWU Effective date: 20081024 |
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Effective date of registration: 20081024 Address after: Beijing city Haidian District minzhuang Road No. 3 Yuquan Huigu Park Building No. 3 zip code: 100195 Patentee after: Beijing Funghan Engineering Consulting Co., Ltd. Address before: Beijing City, Chaoyang District Road No. 2 building 111 room love zip code: 100016 Co-patentee before: Xu Yaowu Patentee before: Wang Wei |
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Effective date of registration: 20081226 Address after: 16 floor, block B, Botai center, 122 South Lake Park, Chaoyang District, Beijing, zip code: 100102 Co-patentee after: Beijing Funghan Engineering Consulting Co., Ltd. Patentee after: Beijing Hefeng Far East Technology Co., Ltd. Address before: Beijing city Haidian District minzhuang Road No. 3 Yuquan Huigu Park Building No. 3 zip code: 100195 Patentee before: Beijing Funghan Engineering Consulting Co., Ltd. |
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Owner name: BEIJING HEFENG YUANDONG TECHNOLOGY CO., LTD. Free format text: FORMER OWNER: BEIJING FENGHAN ENGINEERING CONSULTATIVE CO., LTD. Effective date: 20081226 |
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Granted publication date: 20061011 Termination date: 20181116 |
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| CF01 | Termination of patent right due to non-payment of annual fee |