CN105399455A - System and method for producing compound fertilizer by utilizing chemical engineering tail gas - Google Patents
System and method for producing compound fertilizer by utilizing chemical engineering tail gas Download PDFInfo
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Abstract
The invention discloses a system and method for producing compound fertilizer by utilizing chemical engineering tail gas. The system comprises an ammonia evaporation unit, an ammonium nitrate solution preparation unit and a nitro-compound fertilizer preparation unit which are connected in sequence. The ammonia evaporation unit mainly comprises a liquid ammonia buffer tank, a gas ammonia filter and a gas ammonia superheater which are connected in sequence. The ammonium nitrate solution preparation unit mainly comprises a tubular reactor, a neutralizing flash tank and an evaporation device which are connected in sequence. The nitro-compound fertilizer preparation unit is a high tower granulation device. The gas ammonia superheater in the ammonia evaporation unit is connected with the tubular reactor in the ammonium nitrate solution preparation unit, and the evaporation device in the ammonium nitrate solution preparation unit is connected to the high tower granulation device in the nitro-compound fertilizer preparation unit. Melamine tail gas is filtered and heated through the ammonia evaporation unit and then enters the ammonium nitrate solution preparation unit to be prepared into ammonium nitrate solution together with nitric acid, and finally the ammonium nitrate solution enters the nitro-compound fertilizer preparation unit to be prepared into nitro-compound fertilizer.
Description
Technical field
The present invention relates to melamine tail gas comprehensive utilization and nitro-compound fertilizer production field, particularly relate to the system and method producing ammonium nitrate and nitro-compound fertilizer.
Background technology
At present, domestic urea production capacity is seriously superfluous, and trimeric cyanamide becomes the selection of development urea derived product, but melamine tail gas is treated as the matter of utmost importance of melamine plant development.Melamine tail gas is returned carbamide production system and is added urea middle low-pressure system load, and production bicarbonate of ammonia economic benefit is not good, and production soda ash and ammonium chloride complementary conditions require high.
Advanced and mature production technology is had both at home and abroad on nitro-compound fertilizer.External Technology is deliver in the ammonium nitrate phosphorus melting liquid bath of granulation tower top with gas delivery equipment by phosphate fertilizer or potash fertilizer substantially, through stirring melting, enters prilling tower granulation, form granular complex fertilizer product, but external technology introduction expense is relatively high.Domestic employing part slurry process production technique is simple, but floor space is large, long flow path, rotating machinery are many, power consumption is large, ammonia effusion rate is higher, operating environment is poor; Pellet granulation production technique granulation balling ratio, generally between 35%-60%, should not produce the Chemical Mixed Fertilizer of high nitrogen kind, and general (N) is not more than 18%, and this technique returning charge is than high, and returning charge amount is about 2.5 times of product; High tower prilling technique is widely used in the production of ammonium nitrate phosphorus, ammonium nitrate, nitrophosphate fertilizer, has then just started to relate in nitro compound fertilizer is produced.
Usual melamine tail gas is used for urea production, when producing urea by melamine tail gas, easily causes the pressure instability of urea production process, thus affects the production of urea.
Summary of the invention
Be worth produce nitro-compound fertilizer product simultaneously to play triamine tail gas, the invention provides one and utilize melamine tail gas and preparation of nitric acid ammonium nitrate, then with the system of " high tower prilling " technique coproduction nitro-compound fertilizer.Present invention also offers a kind of method utilizing chemical industry tail gas production composite fertilizer.
For achieving the above object, technical scheme of the present invention is:
Utilize a system for chemical industry tail gas production composite fertilizer, comprise connect successively ammonia evaporation element, ammonium nitrate solution prepares unit and nitro-compound fertilizer prepares unit;
Described ammonia evaporation element mainly comprises the liquefied ammonia surge tank, gas ammonia strainer and the gas ammonia superheater that connect successively;
Described ammonium nitrate solution prepare unit mainly comprise connect successively tubular reactor, in and flash drum and evaporation unit;
It is high tower prilling device that described nitro-compound fertilizer prepares unit;
The tubular reactor that gas ammonia superheater in described ammonia evaporation element and described ammonium nitrate solution are prepared in unit is connected, and the evaporation unit that described ammonium nitrate solution is prepared in unit is connected with the high tower prilling device that described nitro-compound fertilizer is prepared in unit;
Melamine tail gas is filtered through ammonia evaporation element, heating, then enters ammonium nitrate solution and prepares unit and become ammonium nitrate solution with preparation of nitric acid, finally enters nitro-compound fertilizer and prepares unit and be prepared into nitro-compound fertilizer.
The melamine tail gas pressure of the system of entering can be stablized in liquefied ammonia surge tank, countercurrent reaction is carried out with salpeter solution in tubular reactor, not only reduce the reaction times of melamine tail gas and nitric acid, and can pressure in stable system, in and flash drum tail gas remaining after reaction neutralized steam, with further stable system pressure, then through pervaporation, granulation becomes nitro-compound fertilizer, ensure that melamine tail gas carries out the pressure stability of producing within the system by the acting in conjunction of said apparatus, thus ensure that the production of melamine tail gas recycling and nitro-compound fertilizer.
Utilize tubular reactor, the unit volume throughput of melamine tail gas and nitric acid is improved, thus improve the transformation efficiency of melamine tail gas, the ammonium nitrate solution of preparation is by high tower prilling device, achieve three-waste free discharge, cleaner production, reduction energy consumption, improve the productive rate of nitro-compound fertilizer, ensure that the efficiency utilization of melamine tail gas simultaneously, reduce production cost.
Preferably, the import of described liquefied ammonia surge tank connects liquid ammonia ball tank.When melamine tail gas does not meet production, can continue to produce with liquefied ammonia.
Preferred further, the import of the liquefied ammonia outlet connecting fluid ammonia evaporator of described liquefied ammonia surge tank, the described waste of liquefied ammonia surge tank is connected the import of discharge evaporator with the waste of liquid ammonia evaporator, the gas ammonia outlet of described liquid ammonia evaporator is all connected with the import of liquefied ammonia surge tank with the gas ammonia outlet of discharge evaporator, and the waste of described discharge evaporator connects Sewage treatment systems.The utilising efficiency of liquefied ammonia can be improved.
Preferably, described evaporation unit is the first flash vaporization groove connected successively, first vaporizer and whole vaporizer, wherein, described just flash vaporization groove with described in be connected with flash drum, described whole vaporizer is connected with described high tower prilling device.First flash vaporization groove, for steaming the ammonia etc. carried secretly in solution, is avoided entering vaporizer and is caused evaporator pressure excessive and affect production system and stablize.First vaporizer is used for initial concentration liquid, evaporates most moisture, provides the middle product of higher concentration, both can obtain the composition of part external application.Whole vaporizer is used for further concentrated liquid, reaches high density melt liquid.First vaporizer and whole vaporizer combined utilization, can make full use of heat energy evaporation concentration, be convenient to control evaporator process constant respectively, improves efficiency and the effect of evaporation.
Preferred further, the waste vapour outlet of described whole vaporizer is connected with the import of vapor seperator, and the taphole of described whole vaporizer is connected with described high tower prilling device.The waste vapour that whole vaporizer produces is utilized, improves waste vapour and utilize, reduce the discharge of waste.
Further preferred, the import of described vapor seperator exports with the waste vapour of first vaporizer and is connected, and the taphole of described just vaporizer is connected with the import of whole vaporizer.The waste vapour that first vaporizer produces is utilized, improves waste vapour and utilize, reduce the discharge of waste.
Preferably, described ammonium nitrate solution is prepared unit and is washed unit be connected with neutralization; Described neutralization washing unit is the humidifier and steaming tower that connect successively, described humidifier import with described in be connected with flash drum pneumatic outlet, be connected with evaporation unit with flash tank liquid outlet in described, described steaming tower outlet is connected with steam pipe system.Can recycle the ammonia be mingled with in steam and ammonium nitrate, improve the productive rate of raw material, improve waste vapour simultaneously and utilize, reduce the discharge of waste.
Further preferred, described steaming tower liquid exit with described in be connected with flash drum import, described steaming tower pneumatic outlet is connected with steam pipe system.In recovery and time produce ammonium nitrate solution, to improve the utilization ratio of raw material, reduce production cost.
Utilize a method for chemical industry tail gas production composite fertilizer, the steps include:
1) melamine tail gas is successively by entering reactor after filtration, heat treated;
2) the melamine tail gas neutralization reaction of pressurize with nitric acid in the reactor after process generates ammonium nitrate solution, and by the ammonium nitrate solution evaporation concentration generated, the steam of generation washs through neutralization and removes;
3) ammonium nitrate solution after concentrating adopts high tower fused melt granulated technique to be prepared into nitro-compound fertilizer.
Preferably, when trimeric cyanamide is not enough, utilizes liquefied ammonia to generate, the steps include:
1) liquefied ammonia is successively by entering reactor after filtration, heat treated;
2) after process, the neutralization reaction of pressurizeing with nitric acid in the reactor of liquefied ammonia generates ammonium nitrate solution, and by the molten evaporation concentration of ammonium nitrate generated, the steam of generation is through neutralization washing removing;
3) ammonium nitrate solution after concentrating adopts high tower fused melt granulated technique to be prepared into nitro-compound fertilizer.
Its concrete steps are:
1. in liquefied ammonia surge tank, liquefied ammonia enters into liquid ammonia evaporator under gravity, gas ammonia is evaporated with the recirculated water heat exchange in tubulation, gas ammonia turns back to liquefied ammonia surge tank and enters gas ammonia strainer (except impurity such as degreasings) again, enters tubular reactor further by between gas ammonia superheater tubulation pipe after low-pressure saturated steam heating (110-120 DEG C); Liquefied ammonia surge tank, ammonia evaporator bottom water and greasy dirt are discharged to discharge evaporator low-pressure steam heating evaporation through blow-off line, the gas ammonia evaporated turns back to liquefied ammonia surge tank, residue drains into underground sewer through blowdown drum, then enters treatment center of sewage and process;
2. in tubular reactor, nitric acid (58-60%) with purification heat after gas ammonia counter current contact (0.4-0.5MPa, 175-180 DEG C) reaction generate ammonium nitrate, through in and flash tank dodge after steaming obtain ammonium nitrate solution (≤75%); Ammonium nitrate solution (≤75%) successively through ammonium nitrate medial launder, first flash vaporization groove, first vaporizer and whole vaporizer, concentrate the ammonium nitrate solution obtaining 99%; The waste vapour that first vaporizer and whole vaporizer produce is discharged from top and is entered vapor seperator condensation separation, and the boiled off liquor that condensation is got off can be used for evaporation liquefied ammonia thermal source; In and the process steam that produces of flash tank, first flash vaporization groove and vapor seperator discharge from top, enter washing tower;
3. first process steam enters humidifier (being Venturi scrubber), the technique superheated vapour (when about 175 DEG C/gas ammonia is produced during triamine End gas production 185 DEG C) entering washing tower is dropped to temperature of saturation (138.35 DEG C) lower the temperature and carry out pre-wash, maintain circulation by detergent circulator, add nitric acid needed for postreaction in washings and ammonia is carried out absorbing and neutralizing;
4. 99% ammonium nitrate solution is through being metered into granulation tower top tempering tank; mix instantaneously with the solid materials such as powdery monoammonium phosphate, rhombspar, potassium sulfate being promoted to tower top; the low temperature eutectic slip be mixed to form is whitewashed at top of tower; in the granulation of differential rotating granulation machine, tower, naturally cooling balling-up obtains compound fertilizer granules; deliver to powder flow cooler after being collected by the recovering hopper at the bottom of tower and carry out cooling twice; abundant cooled compound fertilizer granules, after screening and surperficial anti-caking process, becomes finished product composite fertilizer through packaging.
Differential two-speed rotary granulating machine overlaps independently transmission rig and feeder system and electrical equipment control by two and forms, each transmission rig carries out stepless control to its rotating speed with turning to by corresponding variable-frequency power sources, Liang Tao mechanism differential work on same axle center (also can synchronously), the a set of responsible each spray orifice full-bodied composite molten liquid with solid phase particles being averagely allocated to granulation differential rotating granulation shower nozzle, another set of, be responsible for fused solution to penetrate in differential rotating granulation shower nozzle, the fused solution of injection meets the spheroidal particle that atmospheric drag fracture is shrunk to certain diameter scope.Full-bodied fused solution very easily blocks the spray orifice of granulation differential rotating granulation shower nozzle, therefore the large ability long period that the spray orifice of granulation differential rotating granulation shower nozzle can only be tried one's best is not blocked to meet quantity-produced requirement, large spray orifice also must can produce the spheroidal particle of the certain diameter scope of processing requirement.The granulation principle of differential granulation uniqueness can make the particle being fractured into D/2 sphere diameter from the fluid column of D diameter spray orifice injection, and common prilling process then can not accomplish this point.
Beneficial effect of the present invention:
(1) solve the difficult environmental issue of triamine tail gas, tail gas obtains recycling simultaneously, improves energy utilization rate.
(2) high tower prilling technique is advanced, unit Forced Mixing, and its mixture homogeneity is good, not sticky equipment.
(3) prilling tower is furnished with multistage refrigerating unit, guarantees that product does not lump, and keeps loose.
(4) this device is furnished with nitro compound fertilizer dry method device for recovering powder, reclaims powder and can be used as factory of composite fertilizer raw material.
(5) melt pelletization takes full advantage of the heat that ammonium nitrate fused solution produces, and blend melt moisture content is low, without the need to drying process, saves mass energy;
(6) can produce the nitro azophoska compound fertilizer of high nitrogen, high density, product particle smooth surface, qualification rate is high, prevented from caking, and the market competitiveness is strong;
(7) three-waste free discharge.
Accompanying drawing explanation
Fig. 1 is system architecture schematic diagram of the present invention;
Fig. 2 is ammonia evaporation element schema;
Fig. 3 is that ammonium nitrate solution prepares unit schema;
Fig. 4 is neutralization washing unit schema;
Fig. 5 is that nitro-compound fertilizer prepares unit flow process;
Fig. 6 is ammonium nitrate solution concentration technology FB(flow block);
Fig. 7 is the whole evaporization process process flow sheet of nitro-compound fertilizer;
Fig. 8 is nitro-compound fertilizer solid material delivery technology schema;
Fig. 9 is that the screening of nitro-compound fertilizer finished product coldly removes procedure technology schema;
Figure 10 is nitro-compound fertilizer packaging process process flow sheet;
Wherein, I, ammonia evaporation element, II, ammonium nitrate solution prepares unit, III, nitro-compound fertilizer prepares unit, and IV, neutralization washing unit, 1, liquefied ammonia surge tank, 2, liquid ammonia evaporator, 3, gas ammonia strainer, 4, discharge evaporator, 5, gas ammonia superheater, 6, tubular reactor, 7 blowdown drums, 8, liquid ammonia ball tank, 9, in and flash tank, 10, ammonium nitrate tundish, 11, first flash vaporization groove, 12, first vaporizer, 13, whole vaporizer, 14, 99% ammonium nitrate solution groove, 15, vapor seperator, 16, evaporative condenser liquid bath, 17, steaming tower, 18, proportioning belt, 19, tempering tank, 20, prilling tower, 21, powder flow cooler, 22, first vapor seperator, 23, first vaporizer-condenser, 24, 92% ammonium nitrate solution groove, 25, raw material storage, 26, feed opening, 27, rotary conveyor, 28, crusher, 29, first lift, 30 vibratory screening apparatuss, 31, raw material feed bin, 32, measuring belt, 33, second lift, 34, 3rd lift, 35, returning charge feed bin, 36, first belt, 37, second belt, 38, 4th lift, 39, 3rd belt, 40, one-level trommel screen, 41, 5th lift, 42, two stage cylinder sieves, and 43, coating cylinder, 44, 6th lift, 45, finished goods warehouse, 46, first pack-thread, 47, second pack-thread, 48, finished product storehouse.
Embodiment
As shown in Figure 1, a kind of system utilizing chemical industry tail gas production composite fertilizer, comprise connect successively ammonia evaporation element I, ammonium nitrate solution prepares unit II and nitro-compound fertilizer prepares unit III, nitro-compound fertilizer prepares unit III and the connection of neutralization washing unit IV;
As shown in Figure 2, ammonia evaporation element I mainly comprises the liquefied ammonia surge tank 1, gas ammonia strainer 3 and the gas ammonia superheater 5 that connect successively; The import of liquefied ammonia surge tank 1 connects liquid ammonia ball tank 8, the import connecting fluid ammonia evaporator 2 of liquefied ammonia surge tank 1, liquefied ammonia surge tank 1 is connected discharge evaporator 4 with the outlet of liquid ammonia evaporator 2, the outlet of discharge evaporator 4 connects liquefied ammonia surge tank 1 and blowdown drum 7 respectively, and gas ammonia superheater 5 connects tubular reactor 6.
As shown in Figure 3, ammonium nitrate solution prepare unit II mainly comprise connect successively tubular reactor 6, in and flash drum 9, ammonium nitrate medial launder 10 and evaporation unit; Evaporation unit is the first flash vaporization groove 11, first vaporizer 12 and the whole vaporizer 13 that connect successively, whole vaporizer 13 connects 99% ammonium nitrate solution groove 14 and vapor seperator 15, being connected with evaporative condenser liquid bath 16 with first vaporizer 12 respectively of vapor seperator 15 respectively.
As shown in Figure 5, nitro-compound fertilizer prepares unit III for high tower prilling device, mainly comprises the 99% ammonium nitrate solution groove 14, tempering tank 19, prilling tower 20 and the powder flow cooler 21 that connect successively, prepares burden to be delivered to tempering tank 19 by proportioning belt 18.
As shown in Figure 4, neutralization washing unit IV be the humidifier and steaming tower 17 that connect successively, steaming tower 17 with in be connected with flash drum 9.
The detailed process utilizing melamine tail gas to produce nitro-compound fertilizer is:
1. melamine tail gas reclaims and ammonium nitrate solution preparation
As shown in Figure 2, melamine tail gas enters into ammonium nitrate solution by liquefied ammonia surge tank 1, gas ammonia strainer 3 and gas ammonia superheater 5 successively and prepares unit II; Then in pressurizeing in tubular reactor 6 with the dust technology (58-60%) from nitric acid plant and generate ammonium nitrate solution, concentration ammonium nitrate solution (≤75%) is obtained with flash tank 9 flash distillation in the ammonium nitrate solution warp generated, ammonium nitrate solution (≤75%) through being pumped to ammonium nitrate medial launder 10 and first flash vaporization groove 11, the process steam produced discharges neutralization washing unit IV from first flash vaporization groove 11 top, as shown in Figure 3.
2. ammonia evaporation
When melamine tail gas can not meet production, draw liquefied ammonia from garden synthetic ammonia installation and produce.
As shown in Figure 2, liquefied ammonia from liquid ammonia ball tank 8 enters liquefied ammonia surge tank 1, in liquefied ammonia surge tank 1, liquefied ammonia enters into liquid ammonia evaporator 2 (between tubulation) under gravity, the gas ammonia that liquefied ammonia between tubulation and the recirculated water heat exchange in tubulation evaporate turns back to liquefied ammonia surge tank 1 again, the gas ammonia going out liquefied ammonia surge tank 1 enters gas ammonia strainer 3 except impurity such as degreasings, filtered gas ammonia enters in gas ammonia superheater tubulation, and the low-pressure saturated steam through between tubulation is heated to 110-120 DEG C and removes ammonium nitrate solution preparation system.Liquefied ammonia surge tank 1, liquid ammonia evaporator 2 bottom water and greasy dirt are discharged to discharge evaporator 4 low-pressure steam heating evaporation through blow-off line, the gas ammonia evaporated turns back to liquefied ammonia surge tank 1, residue drains into underground sewer through blowdown drum 7, then enters treatment center of sewage and process.
3. in and washing
As shown in Figure 3, the process steam (comprising indifferent gas in tail gas) coming self-neutralization flash tank 9 top enters steaming tower 17, so that the ammonium nitrate carried secretly in reclaiming and in steam and free ammonia.
First process steam containing ammonia and ammonium nitrate enters humidifier (being Venturi scrubber), the technique superheated vapour (when about 175 DEG C/gas ammonia is produced during triamine End gas production 185 DEG C) entering steaming tower 17 is dropped to temperature of saturation (138.35 DEG C) lower the temperature and carry out pre-wash, maintain circulation by detergent circulator, add nitric acid needed for postreaction in washings and ammonia is carried out absorbing and neutralizing.
Process steam saturated after humidifier washing is entered in tower by sparger at the bottom of tower and proceeds washing, and washings maintains circulation by pump.Ammonium nitrate drop is by the bottom of gravity separation to tower, and washings returns in washing tower, with flash tank 9 during unnecessary washings turns back to.Ammonium nitrate still containing trace in the washed secondary steam of bubble cap plate, adopts high efficiency demister again to carry out high purification, and ensure that ammonia wherein and ammonium nitrate do not exceed standard, the clean secondary steam after demist delivers to steam pipe system.
4. solution concentrates
As shown in Figure 6, ammonium nitrate solution (≤75% in first vaporizer 12 is entered from first flash vaporization groove 11) and from the ammonium nitrate solution mixing after sewage disposal, mixed nitrate ammonium solution enters to first vaporizer 12 at the flows by action from gravity, along first vaporizer 12 tubulation inner tubal wall nature film forming, the moisture content in heating evaporation ammonium nitrate solution is carried out with steam between pipe, the ammonium nitrate solution of 92% is obtained through one section of evaporation, deliver to 92% ammonium nitrate solution groove 24, again concentrating through being pumped to whole vaporizer 13 ammonium nitrate solution obtaining 99%, delivering to 99% ammonium nitrate solution groove 14.Vapor seperator 22 at the beginning of the waste vapour that first vaporizer 12 produces enters is separated, first vaporizer-condenser 23 cools, and the boiled off liquor that condensation is got off enters evaporative condenser liquid bath 16.To sum up, ammonium nitrate solution (≤75%) ammonium nitrate solution of 92% and 99% is finally produced through first vaporizer and whole evaporator evaporation, participate in batching.
Whole evaporization process as shown in Figure 7, from first vaporizer 12 92% ammonium nitrate solution deliver to 92% ammonium nitrate solution groove 24, deliver in whole vaporizer 13 by 92% ammonium nitrate solution groove 24, reach 99% by the ammonium nitrate solution concentration after whole vaporizer 13 evaporates after 99% ammonium nitrate solution groove 14, deliver to tempering tank 19 production composite fertilizer.
5. nitro-compound fertilizer technical process
As shown in Figure 5, the ammonium nitrate solution sent here by ammonium nitrate operation delivers to 99% ammonium nitrate solution groove 14, prilling tower 20 tower top is pumped into through being metered into tempering tank 19 through ammonium nitrate solution, with the powdery monoammonium phosphate being promoted to tower top through proportioning belt 18, rhombspar, the solid materialss such as potassium sulfate mix instantaneously, the low temperature eutectic slip be mixed to form carries out spray granulating at prilling tower 20 top of tower, naturally cooling is carried out in tower, compound fertilizer granules through cooling balling-up is delivered to powder flow cooler 21 after being collected by the recovering hopper at the bottom of tower and is carried out cooling twice, abundant cooled compound fertilizer granules is after screening and surperficial anti-caking process, finished product composite fertilizer is become through packaging.
Solid materials conveying operation as shown in Figure 8, according to formula instruction by each monoammonium phosphate, potassium sulfate, ground dolomite, each related raw material feed opening 26 is transported to from raw material storage 25 outbound forklift, each feed opening 26 is dosed into after manually unpacking, mixing rotary conveyor 27 is transported to through metering, after crusher 28 coarse breaking, rise to vibratory screening apparatus 30 through the first lift 29 sieve, the bulk raw of sifting out returns thick the breaking of crusher 28 and carries out fragmentation again, promote, meet fineness requirement by Cemented filling to raw material feed bin 31, upper tower lift 33 is transported to through measuring belt 32, be delivered to tempering tank 19, then prilling tower 20 is transported to.
Finished product screening refrigerating work procedure as shown in Figure 9, the compound fertilizer granules sent at the bottom of tower is transported to out tower first belt 37, then be transported to finished product lift 38, exported by finished product lift 38 and be transported to the second belt 39, be then transported to one-level trommel screen 40 and once sieve, the returning charge not meeting granularity requirements of sifting out, be transported to return conveyer 36, be transported to returning charge feed bin 35 through return conveyer 36, through metering, tempering tank 19 is risen to, as material again granulation by the second lift 34.
The finished product meeting granularity requirements sifted out is divided through one-level trommel screen 40 one-level, rise to powder flow cooler 21 by the 3rd lift 41 to cool, then secondary screening is carried out at two stage cylinder sieve 42, the returning charge that secondary sifts out is transported on the return conveyer 36 of one-level screening by rotary conveyor, is transported to returning charge feed bin 35 together with the returning charge that one-level is sifted out.By the qualified finished product that secondary sieves, wrap up anti-hard caking agent through metering, coating cylinder 43, be then transported to subsequent processing packaging post.
As shown in Figure 10, coating compound fertilizer finished product is transported to the 4th lift 44 to packaging process, rises to finished product bin 45, and finished product bin 45 designs two feed openings, and point two fully-automatic packaging line first pack-threads 46 and the second pack-thread 47 carry out being packaged into bagged product.Then by rotary conveyor, bagged product is transported to finished product storehouse 48 and carries out shipping.
By reference to the accompanying drawings the specific embodiment of the present invention is described although above-mentioned; but the restriction not to invention protection domain; one of ordinary skill in the art should be understood that; on the basis of technical scheme of the present invention, those skilled in the art do not need to pay various amendment or distortion that creative work can make still in protection scope of the present invention.
Claims (10)
1. utilize a system for chemical industry tail gas production composite fertilizer, it is characterized in that, comprise connect successively ammonia evaporation element, ammonium nitrate solution prepares unit and nitro-compound fertilizer prepares unit;
Described ammonia evaporation element mainly comprises the liquefied ammonia surge tank, gas ammonia strainer and the gas ammonia superheater that connect successively;
Described ammonium nitrate solution prepare unit mainly comprise connect successively tubular reactor, in and flash drum and evaporation unit;
It is high tower prilling device that described nitro-compound fertilizer prepares unit;
The tubular reactor that gas ammonia superheater in described ammonia evaporation element and described ammonium nitrate solution are prepared in unit is connected, and the evaporation unit that described ammonium nitrate solution is prepared in unit is connected with the high tower prilling device that described nitro-compound fertilizer is prepared in unit;
Melamine tail gas is filtered through ammonia evaporation element, heating, then enters ammonium nitrate solution and prepares unit and become ammonium nitrate solution with preparation of nitric acid, finally enters nitro-compound fertilizer and prepares unit and be prepared into nitro-compound fertilizer.
2. a kind of system utilizing chemical industry tail gas production composite fertilizer as claimed in claim 1, is characterized in that, the import of described liquefied ammonia surge tank connects liquid ammonia ball tank.
3. a kind of system utilizing chemical industry tail gas production composite fertilizer as claimed in claim 2, it is characterized in that, the import of the liquefied ammonia outlet connecting fluid ammonia evaporator of described liquefied ammonia surge tank, the described waste of liquefied ammonia surge tank is connected the import of discharge evaporator with the waste of liquid ammonia evaporator, the gas ammonia outlet of described liquid ammonia evaporator is all connected with the import of liquefied ammonia surge tank with the gas ammonia outlet of discharge evaporator, and the waste of described discharge evaporator connects Sewage treatment systems.
4. a kind of system utilizing chemical industry tail gas production composite fertilizer as claimed in claim 1, it is characterized in that, described evaporation unit is the first flash vaporization groove connected successively, first vaporizer and whole vaporizer, wherein, described just flash vaporization groove with described in be connected with flash drum, described whole vaporizer is connected with described high tower prilling device.
5. a kind of system utilizing chemical industry tail gas production composite fertilizer as claimed in claim 4, is characterized in that, the waste vapour outlet of described whole vaporizer is connected with the import of vapor seperator, and the taphole of described whole vaporizer is connected with described high tower prilling device.
6. a kind of system utilizing chemical industry tail gas production composite fertilizer as claimed in claim 5, it is characterized in that, the import of described vapor seperator exports with the waste vapour of first vaporizer and is connected, and the taphole of described just vaporizer is connected with the import of whole vaporizer.
7. a kind of system utilizing chemical industry tail gas production composite fertilizer as claimed in claim 1, is characterized in that, described ammonium nitrate solution is prepared unit and washed unit with neutralization and be connected; Described neutralization washing unit is the humidifier and steaming tower that connect successively, described humidifier import with described in be connected with flash drum pneumatic outlet, be connected with evaporation unit with flash tank liquid outlet in described, described steaming tower outlet is connected with steam pipe system.
8. a kind of system utilizing chemical industry tail gas production composite fertilizer as claimed in claim 1, is characterized in that, described steaming tower liquid exit with described in and flash drum import be connected, described steaming tower pneumatic outlet is connected with steam pipe system.
9. utilize a method for chemical industry tail gas production composite fertilizer, it is characterized in that, the steps include:
1) melamine tail gas is successively by entering reactor after filtration, heat treated;
2) the melamine tail gas neutralization reaction of pressurize with nitric acid in the reactor after process generates ammonium nitrate solution, and by the molten evaporation concentration of ammonium nitrate generated, the steam of generation washs through neutralization and removes;
3) ammonium nitrate solution after concentrating adopts high tower fused melt granulated technique to be prepared into nitro-compound fertilizer.
10. a kind of method utilizing chemical industry tail gas production composite fertilizer as claimed in claim 9, is characterized in that, when trimeric cyanamide is not enough, utilizes liquefied ammonia to generate, the steps include:
1) liquefied ammonia is successively by entering reactor after filtration, heat treated;
2) after process, the neutralization reaction of pressurizeing with nitric acid in the reactor of liquefied ammonia generates ammonium nitrate solution, and by the molten evaporation concentration of ammonium nitrate generated, the steam of generation is through neutralization washing removing;
3) ammonium nitrate solution after concentrating adopts high tower fused melt granulated technique to be prepared into nitro-compound fertilizer.
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| CN106432115A (en) * | 2016-12-07 | 2017-02-22 | 合力泰科技股份有限公司 | Melamine production process for co-producing nitro-compound fertilizer |
| CN108178168A (en) * | 2017-12-29 | 2018-06-19 | 新疆中泰化学阜康能源有限公司 | Industrial waste sulfuric acid and the hot method acidolysis device of saltcake and application method |
| CN110818475A (en) * | 2019-12-13 | 2020-02-21 | 太原柏悟化工科技有限公司 | Production method and production device of ammonium nitrate-sulfur compound fertilizer |
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| CN106432115A (en) * | 2016-12-07 | 2017-02-22 | 合力泰科技股份有限公司 | Melamine production process for co-producing nitro-compound fertilizer |
| CN108178168A (en) * | 2017-12-29 | 2018-06-19 | 新疆中泰化学阜康能源有限公司 | Industrial waste sulfuric acid and the hot method acidolysis device of saltcake and application method |
| CN108178168B (en) * | 2017-12-29 | 2020-02-07 | 新疆中泰化学阜康能源有限公司 | Industrial waste sulfuric acid and mirabilite thermal acidolysis device and use method thereof |
| CN110818475A (en) * | 2019-12-13 | 2020-02-21 | 太原柏悟化工科技有限公司 | Production method and production device of ammonium nitrate-sulfur compound fertilizer |
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