CN102491292A - Low-consumption and low-emission nitric acid production method and production equipment thereof - Google Patents
Low-consumption and low-emission nitric acid production method and production equipment thereof Download PDFInfo
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- CN102491292A CN102491292A CN2011103997494A CN201110399749A CN102491292A CN 102491292 A CN102491292 A CN 102491292A CN 2011103997494 A CN2011103997494 A CN 2011103997494A CN 201110399749 A CN201110399749 A CN 201110399749A CN 102491292 A CN102491292 A CN 102491292A
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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
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
The invention discloses a low-consumption and low-emission nitric acid production method and production equipment thereof. The method and the equipment adopts the same low-pressure level for oxidation and absorption, the double-pressurization high-pressure level is omitted, a molecular sieve absorption device is adopted for tail gas treatment of a nitric acid absorption tower, in addition, secondary air is used for taking reaction with nitric oxide absorbed in the molecular sieve absorption device to form regenerated gas, the regenerated gas is sent into the nitric acid absorption tower to be recovered and reutilized, the nitrogen oxide content in the tail gas is lower than 100mg/Nm<3>, in addition, the yield of the nitric acid can also be improved through the recovery and the utilization of regeneration gas, a layer of silk screen is arranged on a sieve plate tower disc of an oxidation section of the nitric acid absorption tower, the oxidation speed at high pressure and low pressure can be effectively accelerated, and an N20 decomposition catalyst layer is also additionally arranged in an oxidation reaction vessel, so the N20 content in the nitric oxide gas in the oxidation reaction vessel can be reduced to about 100PPM. The nitric acid production method does not need to adopt two pressure levels, no nitric oxide compressor is adopted, no tail gas ammonification re-treatment device is adopted, the investment is greatly saved, and the consumption is reduced.
Description
Technical field
The present invention relates to produce the nitric acid technical field, particularly a kind of method and production unit thereof that utilizes ammonia and air to produce nitric acid.
Background technology
(pressure and the absorption pressure that are oxidation are 1.0 to 1.2 Mpa at present both at home and abroad with ammonia and air production nitric acid novel process non-pressure process (be the pressure of oxidation and and absorption pressure is a normal pressure), middle-pressure process (pressure and the absorption pressure that are oxidation are 0.3 to 0.4 Mpa) and high-pressure process to be arranged;); And the two platen press nitric acid production technologies of state-of-the-art genus; The pressure that promptly is oxidation is 0.4 to 0.5 Mpa; And absorption pressure is 1.0 to 1.2 Mpa, and it can make that the platinum consumption of oxidation is lower, and the also low purpose of the nitrogen oxide of exhaust emissions.The subject matter of two platen press nitric acid production technologies is:
(1), must nitrogen oxide gas be recompressed 1.2 Mpa sends to the absorption operation, nitrogen oxide gas compressor of needs again;
(2), the nitrogen oxide of exhaust emissions has 400mg/Nm
3, do not reach 300 mg/Nm of country
3, discharge index;
(3), in order to reach 300 mg/Nm of country
3, discharge index need increase ammonia selective reaction device at exhaust system usually, with ammonia and nitrogen oxide reaction, generates nitrogen with catalyzer, makes 300 mg/Nm that reach country
3, discharge index;
(4), contain 1000 to the 1500PPM nitrous oxide in the nitrogen oxide gas of oxidation reactor, nitrous oxide is the greenhouse gases of high equivalent weight, and the superficial heat effect of unit mass is CO
2310 times, be the major transaction project of CDM in the world.
Summary of the invention
Goal of the invention of the present invention is: to the problem of above-mentioned existence, providing a kind of has transformation absorption to reclaim that nitrogen oxide utilizes again in the tail gas, and reduces in the tail gas content of nitrogen oxide to most advanced＜100 mg/Nm
3The low consumption of index, the nitric acid preparation method of low emission and production unit thereof.
Technical scheme of the present invention is achieved in that the nitric acid preparation method of a kind of low consumption, low emission, it is characterized in that: may further comprise the steps:
A), air is compressed to 0.4 to 0.6Mpa through air, is divided into two-way by the air air compressed, the one tunnel is primary air, another road is a secondary air;
B), primary air mixes the back and gets into oxidation reactor with ammonia, the ammonia air Mixture is generating the pyroreaction gas that contains nitrogen oxide through the reaction of the platinum catalyst layers in oxidation reactor back, temperature of reaction is 860 ℃ to 900 ℃;
C), the pyroreaction gas process recovery of heat that generates through step b) also gets into nitric acid absorption tower water absorption generation nitric acid in the cooling back;
D), the tail gas of nitric acid absorption tower generation gets into the molecular sieve adsorption device and sloughs the nitrogen oxide in the tail gas, nitrogen oxide＜100 mg/Nm of clean tail gas
3, clean tail gas is again through discharging behind tail gas recycle heat and the recovered energy;
E), secondary air is fed in the molecular sieve adsorption device, make the nitrogen oxide reaction of adsorbing in secondary air and the molecular sieve adsorption device obtain the resurgent gases of high density oxidation nitrogen, then resurgent gases is sent into nitric acid absorption tower and recycle.
The nitric acid preparation method of low consumption of the present invention, low emission, it is in said step b), and the reaction gas that has passed through platinum catalyst layers passes through N again
20 decomposition catalyst layer is with the N in the reaction gas
20 reaction generates nitrogen, makes N in the reaction gas
20 content is reduced to 50 to 100PPM.
The nitric acid preparation method of low consumption of the present invention, low emission; It is in said step c); Pyroreaction gas reclaims heat through waste heat boiler earlier; And to produce temperature be 400 to 500 ℃ of superheated steam, passes through interchanger again, after watercooler is cooled to about 40 ℃, sends in the nitric acid absorption tower at last.
The nitric acid preparation method of low consumption of the present invention, low emission, it is in said step d), and clean tail gas passes through tail gas expansion turbine recovered energy after reclaiming heat through interchanger again, at last through the aiutage discharging.
The nitric acid preparation method of low consumption of the present invention, low emission, its nitric acid that generates through step c) are discharged to send at the bottom of by the nitric acid absorption tower tower and are drifted tower, and the part of secondary air is sent into and drifted in the tower, obtain product nitric acid after sloughing the nitrogen oxide in the nitric acid.
The nitric acid preparation method of low consumption of the present invention, low emission, it is in drifting tower, and the gas that goes out tower behind the nitrogen oxide of secondary air in sloughing nitric acid is sent in the nitric acid absorption tower.
The nitric acid production equipment of a kind of low consumption, low emission; It is characterized in that: comprise the oxidation reactor, interchanger, watercooler and the nitric acid absorption tower that connect successively; In said oxidation reactor, be provided with platinum catalyst layers and waste heat boiler; The inlet mouth of said oxidation reactor is through pipeline and air and ammonia pipeline connection; The exhaust port at said nitric acid absorption tower top is communicated with molecular sieve adsorption device inlet mouth end, and the air outlet end of molecular sieve adsorption device is communicated with interchanger, and said air is communicated with the molecular sieve adsorption device.
The nitric acid production equipment of low consumption of the present invention, low emission, it is provided with N below said oxidation reactor inside, platinum catalyst layers
20 decomposition catalyst layer.
The nitric acid production equipment of low consumption of the present invention, low emission, the sieve tray of its said nitric acid absorption tower oxidation panel is provided with one deck silk screen.
The nitric acid production equipment of low consumption of the present invention, low emission; The bottom of its said nitric acid absorption tower with drift tower and be communicated with; Said exhaust port of drifting top of tower is communicated with nitric acid absorption tower; Said air with drift tower and be communicated with, said interchanger is connected with the tail gas expansion turbine, said tail gas expansion turbine is connected with aiutage.
The present invention adopts oxidation and absorbs same low pressure grade; The high pressure grade of the two pressurizations of cancellation; On the vent gas treatment of nitric acid absorption tower, adopt the molecular sieve adsorption device; And form resurgent gases with the reaction of the nitrogen oxide of secondary air and molecular sieve adsorption device internal adsorption, and send into nitric acid absorption tower again and recycle, not only make content of nitrogen oxide＜100 mg/Nm in the tail gas
3, and the recycling of resurgent gases can also be increased production nitric acid; And the sieve tray of nitric acid absorption tower oxidation panel is provided with one deck silk screen, can effectively improve the oxidation rate under the low pressure; In oxidation reactor, also have additional N
20 decomposition catalyst layer can make N in the interior nitrogen oxide gas of oxidation reactor
20 content is reduced to about 100PPM.This nitric acid preparation method is the nitric acid production technology of a kind of not only environmental protection but also low consumption, and technical process is compact, need not use two pressure ratings, does not have nitrogen oxide gas compressor, does not have tail gas ammonification treatment unit again, has saved investment greatly, has reduced consumption.
Description of drawings
Fig. 1 is a structural principle synoptic diagram of the present invention.
Mark among the figure: 1 is oxidation reactor, and 2 is platinum catalyst layers, and 3 is N
20 decomposition catalyst layer, 4 is waste heat boiler, and 5 is interchanger, and 6 is watercooler, and 7 is nitric acid absorption tower, and 8 for drifting tower, and 9 is air, and 10 is the molecular sieve adsorption device, and 11 is the tail gas expansion turbine, and 12 is aiutage.
Embodiment
Below in conjunction with accompanying drawing, the present invention is done detailed explanation.
In order to make the object of the invention, technical scheme and advantage clearer,, the present invention is further elaborated below in conjunction with accompanying drawing and embodiment.Should be appreciated that specific embodiment described herein only in order to explanation the present invention, and be not used in qualification the present invention.
As shown in Figure 1; The nitric acid production equipment of a kind of low consumption, low emission; Comprise the oxidation reactor 1, interchanger 5, watercooler 6 and the nitric acid absorption tower 7 that connect successively; In said oxidation reactor 1, be provided with platinum catalyst layers 2 and waste heat boiler 4, the inlet mouth of said oxidation reactor 1 is through pipeline and air 9 and ammonia pipeline connection, and the exhaust port at said nitric acid absorption tower 7 tops is communicated with molecular sieve adsorption device 10 inlet mouth ends; The air outlet end of molecular sieve adsorption device 10 is communicated with interchanger 5, and said air 9 is communicated with molecular sieve adsorption device 10; The bottom of said nitric acid absorption tower 7 with drift tower 8 and be communicated with; Said exhaust port of drifting tower 8 tops is communicated with nitric acid absorption tower 7; Said air 9 with drift tower 8 and be communicated with, said interchanger 5 is connected with tail gas expansion turbine 11, said tail gas expansion turbine 11 is connected with aiutage 12.
Wherein, below said oxidation reactor 1 inside, platinum catalyst layers 2, be provided with N
20 decomposition catalyst layer 3, the sieve tray of said nitric acid absorption tower 7 oxidation panels is provided with one deck silk screen.
The nitric acid preparation method of a kind of low consumption, low emission is characterized in that: may further comprise the steps:
A), air is compressed to 0.4 to 0.6Mpa through air, is divided into two-way by the air air compressed, the one tunnel is primary air, another road is a secondary air;
B), primary air mixes back entering oxidation reactor with ammonia; The ammonia air Mixture is generating the pyroreaction gas that contains nitrogen oxide through the reaction of the platinum catalyst layers in oxidation reactor back; Temperature of reaction is 860 ℃ to 900 ℃, and the reaction gas that has passed through platinum catalyst layers passes through N again
20 decomposition catalyst layer is with the N in the reaction gas
20 reaction generates nitrogen, makes N in the reaction gas
20 content is reduced to 50 to 100PPM;
C), the pyroreaction gas that generates through step b) reclaims heat through waste heat boiler earlier; And the generation temperature is 400 to 500 ℃ of superheated steam; Pass through interchanger again, after watercooler is cooled to about 40 ℃, send into water absorption generation nitric acid in the nitric acid absorption tower at last;
D), the tail gas of nitric acid absorption tower generation gets into the molecular sieve adsorption device and sloughs the nitrogen oxide in the tail gas, nitrogen oxide＜100 mg/Nm of clean tail gas
3, clean tail gas passes through tail gas expansion turbine recovered energy after reclaiming heat through interchanger again, at last through the aiutage discharging;
E), secondary air is fed in the molecular sieve adsorption device, make the nitrogen oxide reaction of adsorbing in secondary air and the molecular sieve adsorption device obtain the resurgent gases of high density oxidation nitrogen, then resurgent gases is sent into nitric acid absorption tower and recycle.
Wherein, The nitric acid that generates through step c) is discharged to send at the bottom of by the nitric acid absorption tower tower and is drifted tower; The part of secondary air is sent into and is drifted in the tower, obtains product nitric acid after sloughing the nitrogen oxide in the nitric acid, and; In drifting tower, the gas that goes out tower behind the nitrogen oxide of secondary air in sloughing nitric acid is sent in the nitric acid absorption tower and is recycled.
Nitric acid plants with 1000 tons of day productions is an example: 7300 Kmol/h air are divided into two-way after air is compressed to 0.4 to 0.6 Mpa, the one tunnel is primary air 6200 Kmol/h, and another road is secondary air 1100 Kmol/h.
Primary air mixes the back and gets into oxidation reactor with ammonia 682Kmol/h, the platinum catalyst layers reaction in oxidation reactor generates NO gas, and temperature of reaction is 860 ℃ to 900 ℃, and pyroreaction gas is at N
2The O catalyst layer is with N
2The O reaction generates nitrogen, and makes N
2O content is reduced to about 100PPM; Earlier to reclaim heat through waste heat boiler and produce temperature be 400 to 500 ℃ steam to pyroreaction gas then, passes through interchanger again, is cooled to about 40 ℃ at watercooler at last and sends into nitric acid absorption tower.
Water 9000 kg/h absorb and generate nitric acid in nitric acid absorption tower; The gas tail gas that goes out nitric acid absorption tower is approximately 5820 Kmol/h; Nitric acid at the bottom of the nitric acid absorption tower tower is sent into and is drifted tower, obtains product nitric acid 41700kg/h after utilizing the part of secondary air to slough the nitrogen oxide in the nitric acid.
The tail gas that goes out nitric acid absorption tower is sloughed nitrogen oxide gas earlier in the molecular sieve adsorption device, the nitrogen oxide of clean tail gas<100 mg/>Nm
3, and then through after interchanger reclaims the heat in the clean tail gas, at last behind tail gas expansion turbine recovered energy, through the aiutage discharging.
Wherein another part of secondary air is sent in the molecular sieve adsorption device and is formed the resurgent gases that contains high density oxidation nitrogen with being adsorbed the nitrogen oxide reaction, resurgent gases is sent into nitric acid absorption tower recycle raising the output nitric acid.
The above is merely preferred embodiment of the present invention, not in order to restriction the present invention, all any modifications of within spirit of the present invention and principle, being done, is equal to and replaces and improvement etc., all should be included within protection scope of the present invention.
Claims (10)
1. the nitric acid preparation method of a low consumption, low emission is characterized in that: may further comprise the steps:
A), air is compressed to 0.4 to 0.6Mpa through air, is divided into two-way by the air air compressed, the one tunnel is primary air, another road is a secondary air;
B), primary air mixes the back and gets into oxidation reactor with ammonia, the ammonia air Mixture is generating the pyroreaction gas that contains nitrogen oxide through the reaction of the platinum catalyst layers in oxidation reactor back, temperature of reaction is 860 ℃ to 900 ℃;
C), the pyroreaction gas process recovery of heat that generates through step b) also gets into nitric acid absorption tower water absorption generation nitric acid in the cooling back;
D), the tail gas of nitric acid absorption tower generation gets into the molecular sieve adsorption device and sloughs the nitrogen oxide in the tail gas, nitrogen oxide＜100 mg/Nm of clean tail gas
3, clean tail gas is again through discharging behind tail gas recycle heat and the recovered energy;
E), secondary air is fed in the molecular sieve adsorption device, make the nitrogen oxide reaction of adsorbing in secondary air and the molecular sieve adsorption device obtain the resurgent gases of high density oxidation nitrogen, then resurgent gases is sent into nitric acid absorption tower and recycle.
2. the nitric acid preparation method of low consumption according to claim 1, low emission is characterized in that: in said step b), the reaction gas that has passed through platinum catalyst layers passes through N again
20 decomposition catalyst layer is with the N in the reaction gas
20 reaction generates nitrogen, makes N in the reaction gas
20 content is reduced to 50 to 100PPM.
3. the nitric acid preparation method of low consumption according to claim 2, low emission; It is characterized in that: in said step c); Pyroreaction gas reclaims heat through waste heat boiler earlier; And to produce temperature be 400 to 500 ℃ of superheated steam, passes through interchanger again, after watercooler is cooled to about 40 ℃, sends in the nitric acid absorption tower at last.
4. the nitric acid preparation method of low consumption according to claim 3, low emission is characterized in that: in said step d), clean tail gas passes through tail gas expansion turbine recovered energy after reclaiming heat through interchanger again, at last through the aiutage discharging.
5. according to the nitric acid preparation method of any described low consumption, low emission in the claim 1 to 4; It is characterized in that: the nitric acid that generates through step c) is discharged to send at the bottom of by the nitric acid absorption tower tower and is drifted tower; The part of secondary air is sent into and is drifted in the tower, obtains product nitric acid after sloughing the nitrogen oxide in the nitric acid.
6. the nitric acid preparation method of low consumption according to claim 5, low emission is characterized in that: in drifting tower, the gas that goes out tower behind the nitrogen oxide of secondary air in sloughing nitric acid is sent in the nitric acid absorption tower.
7. the nitric acid production equipment of a low consumption, low emission; It is characterized in that: comprise the oxidation reactor (1), interchanger (5), watercooler (6) and the nitric acid absorption tower (7) that connect successively; In said oxidation reactor (1), be provided with platinum catalyst layers (2) and waste heat boiler (4); The inlet mouth of said oxidation reactor (1) is through pipeline and air (9) and ammonia pipeline connection; The exhaust port at said nitric acid absorption tower (7) top is communicated with molecular sieve adsorption device (10) inlet mouth end; The air outlet end of molecular sieve adsorption device (10) is communicated with interchanger (5), and said air (9) is communicated with molecular sieve adsorption device (10).
8. the nitric acid production equipment of low consumption according to claim 7, low emission is characterized in that:, platinum catalyst layers (2) below inner at said oxidation reactor (1) is provided with N
20 decomposition catalyst layer (3).
9. according to the nitric acid production equipment of claim 7 or 8 described low consumption, low emission, it is characterized in that: the sieve tray of said nitric acid absorption tower (7) oxidation panel is provided with one deck silk screen.
10. the nitric acid production equipment of low consumption according to claim 9, low emission; It is characterized in that: the bottom of said nitric acid absorption tower (7) with drift tower (8) and be communicated with; Said exhaust port of drifting tower (8) top is communicated with nitric acid absorption tower (7); Said air (9) with drift tower (8) and be communicated with, said interchanger (5) is connected with tail gas expansion turbine (11), said tail gas expansion turbine (11) is connected with aiutage (12).
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| CN2011103997494A CN102491292A (en) | 2011-12-06 | 2011-12-06 | Low-consumption and low-emission nitric acid production method and production equipment thereof |
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| CN2011103997494A CN102491292A (en) | 2011-12-06 | 2011-12-06 | Low-consumption and low-emission nitric acid production method and production equipment thereof |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103230743A (en) * | 2013-04-09 | 2013-08-07 | 内蒙古乌拉山化肥有限责任公司 | Nitrogen oxide tail gas emission reduction method |
| CN103449388A (en) * | 2013-09-10 | 2013-12-18 | 安徽淮化股份有限公司 | Recycling method of dilute nitric acid and special equipment for method |
| CN104310324A (en) * | 2014-10-14 | 2015-01-28 | 河北冀衡赛瑞化工有限公司 | Production method of electric draggable double-pressurizing nitric acid device |
| CN104495768A (en) * | 2015-01-13 | 2015-04-08 | 四川美丰化工股份有限公司 | Method and device for improving ammoxidation rate of nitric acid manufacture |
| CN105366653A (en) * | 2014-08-25 | 2016-03-02 | 蒋小华 | Nitric acid production technology with double-pressurized method |
| CN108698826A (en) * | 2016-02-24 | 2018-10-23 | 卡萨尔公司 | Ammonia oxidation reactor in nitric acid production |
| CN109499357A (en) * | 2018-12-12 | 2019-03-22 | 四川泸天化股份有限公司 | A kind of method of nitrous oxide emission in improvement commercial plant |
| CN114423519A (en) * | 2019-10-25 | 2022-04-29 | 卡萨乐有限公司 | Process and reactor for the catalytic oxidation of ammonia |
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103230743A (en) * | 2013-04-09 | 2013-08-07 | 内蒙古乌拉山化肥有限责任公司 | Nitrogen oxide tail gas emission reduction method |
| CN103230743B (en) * | 2013-04-09 | 2015-11-18 | 内蒙古乌拉山化肥有限责任公司 | A kind of nitrogen oxide tail gas emission method |
| CN103449388A (en) * | 2013-09-10 | 2013-12-18 | 安徽淮化股份有限公司 | Recycling method of dilute nitric acid and special equipment for method |
| CN103449388B (en) * | 2013-09-10 | 2016-03-30 | 安徽淮化股份有限公司 | A kind of dust technology recovery method and specific equipment thereof |
| CN105366653A (en) * | 2014-08-25 | 2016-03-02 | 蒋小华 | Nitric acid production technology with double-pressurized method |
| CN104310324A (en) * | 2014-10-14 | 2015-01-28 | 河北冀衡赛瑞化工有限公司 | Production method of electric draggable double-pressurizing nitric acid device |
| CN104495768A (en) * | 2015-01-13 | 2015-04-08 | 四川美丰化工股份有限公司 | Method and device for improving ammoxidation rate of nitric acid manufacture |
| CN108698826A (en) * | 2016-02-24 | 2018-10-23 | 卡萨尔公司 | Ammonia oxidation reactor in nitric acid production |
| CN109499357A (en) * | 2018-12-12 | 2019-03-22 | 四川泸天化股份有限公司 | A kind of method of nitrous oxide emission in improvement commercial plant |
| CN114423519A (en) * | 2019-10-25 | 2022-04-29 | 卡萨乐有限公司 | Process and reactor for the catalytic oxidation of ammonia |
| CN114423519B (en) * | 2019-10-25 | 2023-10-10 | 卡萨乐有限公司 | Method and reactor for catalytic oxidation of ammonia |
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Application publication date: 20120613 |