CN1299978C - Double-action reinforced diammonium phosphate tail washing technology with triphase gas-powder-fog system - Google Patents
Double-action reinforced diammonium phosphate tail washing technology with triphase gas-powder-fog system Download PDFInfo
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- CN1299978C CN1299978C CNB021280177A CN02128017A CN1299978C CN 1299978 C CN1299978 C CN 1299978C CN B021280177 A CNB021280177 A CN B021280177A CN 02128017 A CN02128017 A CN 02128017A CN 1299978 C CN1299978 C CN 1299978C
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Abstract
The present invention relates to a technology of treating dust containing tail gas of diammonium phosphate (DAP) and a reinforcement technique of gas-powder-fog three-phase mass transfer. The low-grade enthalpy value, the temperature difference, the enthalpy difference and the hygrometric different of tail gas self are used as driving force, the purification degree of tail gas NH3 is improved, and washing flow is simultaneously shortened to improve efficiency. Compared with the prior art (for example, a large-size technological device with the product scale of 84 t/h), the discharge amount of the tail gas whose temperature is higher than 88 DEGC can be reduced by 163[Nm<3>/per ton products], the return amount of washing solution for a DAP system is reduced by 131[kg/ per ton products], and the concentration amount of raw material phosphoric acid is reduced by 12%(the P2O5 content can be from 45 to 48%). The technique can reduce the hot discharge towards the atmospheric air, and the concentration load of the phosphoric acid is reduced. The technique has the characteristics of utilization rate improvement, environmental protection, obvious economic benefit and obvious environmental benefit.
Description
The present invention relates to the treatment process and the gas-powder-fog three-phase heat and mass intensifying technology of diammonium phosphate (DAP) dust-laden tail gas, use gas-powder-fog three-phase economic benefits and social benefits heat and mass transfer enhancement reaction washer of the present invention, tail gas is given a dinner of welcome, ammonia absorbs and the humidification operation is carried out simultaneously, is improving tail gas NH
3In the time of degree of purification, compared with prior art (the large-scale process unit with 84 tons of/hour product scales is an example) can make the exhaust emissions amount more than 88 ℃ reduce 163[Nm
3/ product per ton], washing lotion reduces 131[kg/ product per ton to the DAP system amount of returning], raw material Phosphoric Acid Concentration amount reduces by 12 percentage points of (P
2O
5Content can be 45～48%).This technology had both reduced to atmospheric hot driving, reduced raw material Phosphoric Acid Concentration load again, had the feature, economic benefit and the obvious environment benefit that improve resource utilization and environment protection.
Existing technology from Wet-process Phosphoric Acid Production DAP is to the about 3785[Nm of airborne release tail gas amount
3/ product per ton].With typical [slot type pre-neutralization+add tubular reactor+rotary drum ammoniation-granulation] technology is example, P
2O
5Content is that a concentrated phosphoric acid part of 48～52% directly is neutralized to NH with liquefied ammonia in tubular reactor
3: H
3PO
4Mol ratio reaches 1.8, and another part reacts to NH with gas ammonia in the pre-neutralization groove
3: H
3PO
4Mol ratio reaches 1.4～1.5, sprays into the also additional liquefied ammonia of rotary drum ammoniation granulator simultaneously with slip in two portions and makes overall NH
3: H
3PO
4Mol ratio reaches 1.8.Granulation product is used hot-air dry in moisture eliminator, enter cooling bed cooling back packing again, finally obtains N-P
2O
5Percentage composition is the DAP product of 18-46.
Above-mentioned technological process is washed the absorption system purifying treatment at three respectively from pre-neutralization reactive tank and rotary drum ammoniation granulator effusion gas, dry gas and cooling bed and the gas that gathers dust; its discharge condition is: 88 ℃ of tail gas generated by granulation of reaction, moisture content 0.605kg/kg dry air; 53 ℃ of dried tail gas, moisture content 0.094kg/kg dry air, cooling bed and gather dust 33 ℃ in tail gas, moisture content 0.023kg/kg dry air.Three strands of tail gas the chimney inlet mix with after chimney discharge.
The simple mixing of the fluidic of three strands of temperature, humidity and enthalpy obvious differences is the deadweight loss that a kind of thermodynamic entropy increases, especially when the temperature difference, enthalpy difference and psychrometric difference still can be used in the processes process.
Method disclosed by the invention is, before mixing, above-mentioned tail gas utilizes its temperature difference, enthalpy difference and psychrometric difference are impellent, in gas-powder-fog three-phase dual-purpose reaction washer, carry out heat and mass transfer enhancement by specific processing arrangement, make (comparatively speaking) high temperature, high humidity, the volume of high enthalpy tail gas and quality Yin Wendu reduction and phase transformation are separated out and are reduced, and low temperature, low humidity, the temperature of low enthalpy tail gas, humidity and enthalpy then therefore rise, consequently strengthened the triphasic contact washing effect of gas-powder-fog, increased the steam output of washing tail gas system, can reduce the moisture quantitative limitation of raw material phosphoric acid thereby reduced the washing lotion amount that time is discharged to the DAP system of processing.Method disclosed by the invention had thus both reduced to atmospheric hot driving, reduced raw material Phosphoric Acid Concentration load again, had the feature, economic benefit and the obvious environment benefit that improve resource utilization and environment protection.
Main invention thought of the present invention is to design tail gas treatment process according to the temperature difference, enthalpy difference and psychrometric difference character between the tail gas of DAP process system distinct device discharge, make it directly to contact the partition that hangs down in the reaction washer of economic benefits and social benefits reinforced structure under the temperature difference and conduct heat having the gas-powder-fog three-phase, the end of line air purge dirt of going forward side by side, ammonia absorb and the humidification dehumidification.Two combine into one for high-temperature tail gas decrement and tail gas washing liquid decrement process, is the characteristics on this technological principle.
The present invention compares with prior art (the large-scale process unit with 84 tons of/hour product scales is an example), and principal feature is: 1) the exhaust emissions amount more than 88 ℃ reduces 163[Nm
3/ product per ton], washing lotion reduces 131[kg/ product per ton to the DAP system amount of returning], raw material Phosphoric Acid Concentration amount reduces by 12 percentage points of (P
2O
5Content can be 45～48%).2) the vent gas treatment flow process shortens, and device reduces 1/3.
Technical essential of the present invention is to utilize the temperature difference, enthalpy difference and psychrometric difference between the tail gas that DAP process system distinct device discharges to carry out the partition phase-change heat transfer in the reaction washer with gas-powder-fog three-phase mixing, washing structure, mass transfer and chemical reaction take place between gas-liquid two-phase when tail gas is given a dinner of welcome, and can obtain 6.7 * 10 under 20～30 ℃ of heat transfer temperature difference conditions
6[kJ/m
3Hr] the volume heat-transfer intensity, the tail gas of high temperature, high humidity (comparatively speaking) side is because of cooling, condensation decrement, the ammonia of low temperature, low humidity (comparatively speaking) side gas phase is absorbed and the water of liquid phase is vaporized, thereby realizes tail gas clean-up and the washings evaporation decrement efficient process that two combine into one.
Provide embodiments of the invention below in conjunction with accompanying drawing, and the present invention is described in further detail by embodiment.
Embodiment: [slot type pre-neutralization+add tubular reactor+rotary drum ammoniation-granulation] technology, 600,000 tons of DAP/ (84 tons/hour) product gas washing Decrement Technique
Existing process unit from pre-neutralization reactive tank and rotary drum ammoniation granulator effusion gas, dry gas and cooling bed with gather dust gas respectively after three washing absorption system purifying treatment, the condition before chimney enters the mouth mixing is:
The reaction tail gas generated by granulation: 88 ℃, moisture content 0.605kg/kg dry air, flow 853Nm
3/ product drying tail gas per ton: 53 ℃, moisture content 0.094kg/kg dry air, flow 1268Nm
3/ product the cooling per ton and the tail gas that gathers dust: 33 ℃, moisture content 0.023kg/kg dry air, flow 1664Nm
3/ product tail gas total flux per ton: 3785Nm
3/ product per ton
Present embodiment makes reaction effusion gas (118 ℃ contain: air 18.4Nm
3/ product per ton, water vapour 166.7Nm
3/ product per ton, ammonia 14.3Nm
3/ product per ton) cooling condensation on the heat exchange wall of the first reaction washer, therein through the dry gas of once washing by the secondary washing humidification after as discharging tail gas 1 by induced draft fan suction chimney (60 ℃ contain: air 1102Nm
3/ product per ton, water vapour 225.4Nm
3/ product per ton).Through the cooling condensation decrement, be cooled to reaction end gas and tablets press effusion gas (76 ℃ contain: air 413.8Nm of 95 ℃
3/ product per ton, water vapour 201.0Nm
3/ product per ton, ammonia 23.8Nm
3/ product per ton) is mixed into the second reaction washer and emits reaction heat with dilute phosphoric acid absorption ammonia, and further in the 3rd reaction washer, carry out secondary washing, simultaneously by heat exchange wall cooling condensation decrement, be cooled to 75 ℃ as discharging tail gas 3 by induced draft fan suction chimney (75 ℃ contain: air 432.2Nm
3/ product per ton, water vapour 265.3Nm
3/ product per ton), condensate return to the four washers, washing cooling bed and gather dust gas (57 ℃ contain: air 1606.2Nm
3/ product per ton, water vapour 32.4Nm
3/ product per ton).Cooling bed tail gas after the washing and the tail gas that gathers dust are in the enterprising step washing of the heat exchange wall of the 3rd reaction washer and obtain heat, behind the humidification as discharging tail gas 2 by induced draft fan suction chimney (50 ℃ contain: air 1606.2Nm
3/ product per ton, water vapour 167.7Nm
3/ product per ton).
By present embodiment in conjunction with the accompanying drawings as seen, all secondary washing liquid replenish by containing wet tail gas phlegma, do not have to add washing lotion, so reduced the washing lotion discharging.The secondary washing process is carried out simultaneously in the both sides of heat exchange wall, and strengthening process not only thus, and make the process Highgrade integration has reduced the exhaust emissions temperature and increased saturation ratio under tail gas clean-up degree and the low temperature simultaneously.Therefore shortened tail wash journey, reduced tail and washed equipment.Behind the present embodiment tail gas clean-up, the condition before the chimney inlet mixes is:
Reaction tail gas generated by granulation (discharging tail gas 3): 75 ℃, moisture content 0.371kg/kg dry air, flow 690Nm
3/ product per ton
Dried tail gas (discharging tail gas 1): 60 ℃, moisture content 0.127kg/kg dry air, flow 1328Nm
3/ product per ton
Cooling and the tail gas that gathers dust (discharging tail gas 2): 50 ℃, moisture content 0.065kg/kg dry air, flow 1774Nm
3/ product per ton
Tail gas total flux: 3792Nm
3/ product per ton
From the isolated condensing liquid quantity of tail gas: 131kg/ product per ton
Claims (2)
1. the method for gas-powder-mist three-phase economic benefits and social benefits reinforced diammonium phosphate tail gas disposal is characterized in that using gas-powder-mist three-phase dual-purpose reaction device, carries out simultaneously that tail gas is given a dinner of welcome, ammonia absorbs and humidification dehumidification operation; The reactor exhaust first the reaction washer the heat exchange wall on the cooling condensation decrement, be cooled to 95 ℃ after, be mixed into the second reaction washer, absorb ammonia wherein and emit reaction heat with the tablets press exhaust with dilute phosphoric acid, then the 3rd reaction washer by heat exchange wall cooling condensation decrement, be cooled to 75 ℃ by induced draft fan suction chimney; The moisture eliminator exhaust in the first reaction washer by 60 ℃ of secondary washing humidifications, temperature by induced draft fan suction chimney; Cooling bed and the tail gas that gathers dust is then in the enterprising step washing of the heat exchange wall of the 3rd reaction washer and obtain heat, humidification, is warmed up to 50 ℃ by induced draft fan suction chimney; All secondary washing liquid replenish by containing wet tail gas phlegma, do not have to add washing lotion, make washing lotion reduce 131kg/ product per ton to the DAP system amount of returning, and raw material Phosphoric Acid Concentration amount reduces by 12 percentage points, P
2O
5Content 45～48% gets final product.
2. processing method as claimed in claim 1, its technical characterictic is that the first reaction washer and the 3rd reaction washer have and carry out simultaneously in the both sides of heat exchange wall that tail gas is given a dinner of welcome, ammonia absorbs and the gas-powder-mist three-phase economic benefits and social benefits heat and mass transfer enhancement function of humidification dehumidification operation, and the volume heat-transfer intensity reaches 6.7 * 10 under 20～30 ℃ of heat transfer temperature difference conditions
6KJ/m
3Hr.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB021280177A CN1299978C (en) | 2002-12-12 | 2002-12-12 | Double-action reinforced diammonium phosphate tail washing technology with triphase gas-powder-fog system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB021280177A CN1299978C (en) | 2002-12-12 | 2002-12-12 | Double-action reinforced diammonium phosphate tail washing technology with triphase gas-powder-fog system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1506303A CN1506303A (en) | 2004-06-23 |
| CN1299978C true CN1299978C (en) | 2007-02-14 |
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ID=34231192
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB021280177A Expired - Fee Related CN1299978C (en) | 2002-12-12 | 2002-12-12 | Double-action reinforced diammonium phosphate tail washing technology with triphase gas-powder-fog system |
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|---|---|
| CN (1) | CN1299978C (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5652609B2 (en) * | 1974-12-04 | 1981-12-14 | ||
| JPH049729B2 (en) * | 1984-03-28 | 1992-02-21 | ||
| JP4009729B2 (en) * | 2004-03-01 | 2007-11-21 | 独立行政法人物質・材料研究機構 | Zinc sulfide nanostructure coated with boron nitride film and method for producing the same |
-
2002
- 2002-12-12 CN CNB021280177A patent/CN1299978C/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5652609B2 (en) * | 1974-12-04 | 1981-12-14 | ||
| JPH049729B2 (en) * | 1984-03-28 | 1992-02-21 | ||
| JP4009729B2 (en) * | 2004-03-01 | 2007-11-21 | 独立行政法人物質・材料研究機構 | Zinc sulfide nanostructure coated with boron nitride film and method for producing the same |
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| Publication number | Publication date |
|---|---|
| CN1506303A (en) | 2004-06-23 |
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Granted publication date: 20070214 Termination date: 20100112 |