WO2002051747A1 - Procede de fabrication d'acide nitrique - Google Patents

Procede de fabrication d'acide nitrique Download PDF

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Publication number
WO2002051747A1
WO2002051747A1 PCT/RU2001/000560 RU0100560W WO02051747A1 WO 2002051747 A1 WO2002051747 A1 WO 2002051747A1 RU 0100560 W RU0100560 W RU 0100560W WO 02051747 A1 WO02051747 A1 WO 02051747A1
Authority
WO
WIPO (PCT)
Prior art keywords
azοτa
gas
nitrogen
oxidation
energy
Prior art date
Application number
PCT/RU2001/000560
Other languages
English (en)
Russian (ru)
Inventor
Yury Anisimovich Ivanov
Anatoly Osipovich Kozhevnikov
Mikhail Mikhailovich KARAVAEV
Original Assignee
KARAVAEVA, Evgeniya Alexandrovna
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by KARAVAEVA, Evgeniya Alexandrovna filed Critical KARAVAEVA, Evgeniya Alexandrovna
Publication of WO2002051747A1 publication Critical patent/WO2002051747A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B21/00—Nitrogen; Compounds thereof
    • C01B21/20—Nitrogen oxides; Oxyacids of nitrogen; Salts thereof
    • C01B21/24—Nitric oxide (NO)
    • C01B21/30—Preparation by oxidation of nitrogen

Definitions

  • the process is subject to chemical technology and relates to methods for the transfer of nitrogen oxides and the conversion of nitric acid to them (.).
  • the waste of this material is high raw materials (ammonia, plate) and material costs (specific investment in ammonia and waste).
  • the purpose of the proposed invention is to increase the efficiency of the process due to the reduction of energy and capital expenditures, and also to eliminate the costs.
  • ch ⁇ ⁇ tsess ⁇ a ⁇ ali ⁇ iches ⁇ g ⁇ ⁇ isleniya m ⁇ le ⁇ ulya ⁇ n ⁇ g ⁇ az ⁇ a ⁇ susches ⁇ vlyae ⁇ sya ⁇ d pressure ⁇ dina ⁇ vym (single) s ⁇ s ⁇ adiey abs ⁇ btsii v ⁇ d ⁇ y, ⁇ luchenny ⁇ ⁇ sid ⁇ v az ⁇ a and ene ⁇ giya for ⁇ tsessa ⁇ isleniya ⁇ dv ⁇ di ⁇ sya with ⁇ m gas ne ⁇ s ⁇ eds ⁇ venn ⁇ in z ⁇ nu ⁇ ea ⁇ tsii ⁇ ⁇ s ⁇ nni ⁇ is ⁇ chni ⁇ v.
  • the process of catalytic oxidation of nitrogen is produced when the temperature is below 1000 ° C and when the oxidizer is lowered to a gas phase, it is at a pressure of 2 %.
  • catalysts for the oxidation of nitrogen they use plate alloys with metals and a platinum group for the use of iron oxides, aluminum alloys, and iron oxide
  • the catalysts can be disposed of in a few instances, but the oxidizer is inadequate in all cases, but it doesn’t work.
  • the proposed method of production is carried out in the following way: air, in a predetermined quantity, is compressed due to the necessary pressure: 1, and
  • the absorber (2) of the complete type is discharged with acid from the tank (18).
  • the acid in the tank is transferred from the absorptive column (9).
  • serpentines are available, after which a short supply of energy for the elimination of acid is obtained - the result of the production of CSP.
  • the acid unit is divided by the pressure and the specified concentration of the steam in the ⁇ and will be in the range 130-190 ° ⁇ .
  • the ⁇ in the heating pipe is heat exchanger (3) heated to 150-250 ° ⁇ , to avoid food and food
  • the PS is mixed with air (energy carrier), which is supplied from the heater (step 16). 4
  • the mixture obtained and temperature below 800 ° C is released to the catalytic converter.
  • the quantity of gases supplied by the gas depends on the range of factors - in the main setpoint of the oxidizer in the mixture and the temperature of the
  • the catalyst is available in a few cases, which are also determined by the parameters, activity and selectivity of the catalyst. However, it is not necessary to have the TG temperature transmitter at the outlet of the process below 450 ° C, t. ⁇ .
  • reaction (3) At temperatures below 600 ° C (depending on the selected pressure), reaction (3)
  • the nitric acid that is produced in the complete (9) product through the whitewash (10) is discharged as an industrial and oxidizing agent. Air with nitrogen oxides, acid and water vapor is disposed of in the lower part of the absolute ring (9). 5
  • the acid of 2 concentrations can be absorbed on the unit.
  • an acid with a higher concentration should be used as an oxidizer.
  • Concentration of industrial acid can always be regulated depending on the availability of food.
  • reaction 1 To ensure that the energy of the process of nitrogen oxidation is reduced (reaction 1), a special carrier of the energy carrier is installed (16). At the expense of constant energy (for example, burning of natural gas), the air is heated up to 800 ° ⁇ and is discharged in the process (4).
  • constant energy for example, burning of natural gas
  • Flue gas energy after the heater (16) is used for steam generation (15).
  • the mode and the operating parameters of the preheater are controlled by the predetermined operating mode of the reaction chamber of the process.
  • the proposed scheme allows you to have a wide range of options for its operation.
  • the set temperatures in the process and the saturator are supported by an external heating. Depending on the research phase, the flow rate of gases in the reactor could change.
  • the supplied gases, temperature and pressure were continuously measured by the IPIP devices;
  • the content of nitrogen oxides was determined by chemical analyzes and, in some cases, by spectrometric analyzes.
  • the composition of the acid in the USA and the necessary conditions was shared by chemical analyzes.
  • ⁇ exploration ⁇ waste for the air was 350-1500 l / h standard oil; pressure from 1 to 20 atm, the temperature before catalyzing varied from 600 ° to 800 ° C.
  • Example 1 (Table 1, ⁇ . ⁇ .4). The tightness of the installation has been verified. Ele ⁇ b ⁇ g ⁇ ev ⁇ m ⁇ dnya ⁇ a ⁇ em ⁇ e ⁇ a ⁇ u ⁇ a in ⁇ ea ⁇ e d ⁇ 750 ° C nasy ⁇ i ⁇ ele, za ⁇ lnenn ⁇ m 70% ⁇ z, d ⁇ 80 ° C and line ⁇ dachi P ⁇ S d ⁇ 240 ° C, za ⁇ us ⁇ ae ⁇ sya ⁇ m ⁇ ess ⁇ , v ⁇ zdu ⁇ szhimae ⁇ sya d ⁇ 7.4 a ⁇ m and ⁇ s ⁇ e ⁇ enn ⁇ ⁇ dnimae ⁇ sya pressure a ⁇ a ⁇ a ⁇ a ⁇ us ⁇ an ⁇ v ⁇ i.
  • a temperature of 140 ° C and a gas mixture at an outlet temperature of 750 ° C is interrupted by an outlet temperature of 750 ° C.
  • the established mode was maintained for 2 hours, after which, at the same time (before and after the catalytic converter), gases were used for the con- nection of the nitrogen compounds.
  • Absorbing fluid was water. The absence of nitrous oxide in the gas is subject to spectroscopic analysis.
  • the content of nitrogen oxides was: before the catalytic layer (PS) - 16.03 + 0.23%; at the exit from the layer - 25.50 + 0.2%; the absolute share of nitrogen compounds is 9.5% by volume.
  • the degree of oxidation ⁇ ( ⁇ ) is 31.5%.
  • the number of nitrogen compounds in the experiment was 1082 l / h.
  • the degree of useful use of products from reactions (1) can be reduced to 60% to 85% when the gas content is 17% of acid and 25% to water.
  • the difference in this circuit is that there is a reduction in all stages of the process due to unified pressure in the event of a failure of the circuit.
  • Production units ⁇ were tied to one place of the building and were counted on a single unit of the analogue of the unit 120 - 2 city.
  • the unit of production for the declared method (for example 2, direct) has the advantage of a lower rate of 11.5 to 13.0% of the cost of working expenses and 5 to 8%.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Catalysts (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

L'invention concerne un procédé de fabrication d'oxydes d'azote et de leur transformation en acide nitrique. Selon l'invention, l'oxydation catalytique de l'azote moléculaire se fait sous une pression égale (sans prendre en ligne de compte la résistance de l'équipement et des conduites en aval de l'appareil de contact) à celle au stade d'absorption des oxydes d'azote obtenus avec de l'eau; l'énergie assurant le déroulement du processus endothermique d'oxydation catalytique de l'azote moléculaire est acheminée directement dans la zone de réaction avec le flux des gaz. L'oxydation catalytique de l'azote moléculaire se fait à des températures inférieures à 1000 °C et avec une teneur en oxydant en phase gazeuse en amont du catalyseur inférieure à 10 % vol. des vapeurs HNO(3) + NOX, avec une pression de 25 atm dans le système. On a choisi comme catalyseur d'oxydation de l'azote moléculaire des alliages de platine avec des métaux du groupe de platine ou des catalyseurs à base des oxydes de fer, de cobalt, de chrome, d'aluminium, avec des additifs promoteurs à base de métaux réfractaires. Pour former un flux de gaz avec de l'oxydant, on peut utiliser non seulement l'air atmosphérique mais aussi un mélange gazeux formé lors de l'évacuation de l'acide de production. L'invention permet de réduire les frais énergétiques et les investissements et de simplifier la technologie de fabrication de l'acide nitrique grâce à l'oxydation de l'azote et l'absorption des oxydes d'azote sous une pression sensiblement égale, en absence de circulation des gaz d'échappement, le fluide de transport d'énergie utilisé étant de l'air ou un gaz avec une teneur d'oxygène ne dépassant pas 5 % vol.
PCT/RU2001/000560 2000-12-27 2001-12-25 Procede de fabrication d'acide nitrique WO2002051747A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
RU2000132663 2000-12-27
RU2000132663/12A RU2174946C1 (ru) 2000-12-27 2000-12-27 Способ производства азотной кислоты

Publications (1)

Publication Number Publication Date
WO2002051747A1 true WO2002051747A1 (fr) 2002-07-04

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Application Number Title Priority Date Filing Date
PCT/RU2001/000560 WO2002051747A1 (fr) 2000-12-27 2001-12-25 Procede de fabrication d'acide nitrique

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RU (1) RU2174946C1 (fr)
WO (1) WO2002051747A1 (fr)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3210939A1 (fr) * 2016-02-24 2017-08-30 Casale SA Réacteur d'oxydation d'ammoniac dans la production d'acide nitrique

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4705670A (en) * 1985-09-03 1987-11-10 Hare Louis R O Multiple oxidation nitrogen fixation
RU2070865C1 (ru) * 1995-07-19 1996-12-27 Общество с ограниченной ответственностью "Нитрохим" Способ получения оксидов азота
RU2127224C1 (ru) * 1997-07-09 1999-03-10 Научно-производственная фирма ООО "НИТРОХИМ" Способ производства азотной кислоты

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4705670A (en) * 1985-09-03 1987-11-10 Hare Louis R O Multiple oxidation nitrogen fixation
RU2070865C1 (ru) * 1995-07-19 1996-12-27 Общество с ограниченной ответственностью "Нитрохим" Способ получения оксидов азота
RU2127224C1 (ru) * 1997-07-09 1999-03-10 Научно-производственная фирма ООО "НИТРОХИМ" Способ производства азотной кислоты

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
V.M. OLEVSKOGO: "Proizvodstvo azotmoi kislotty c agregatakh bolshoi edinichnoi moschosti", KHIMIYA, 1985, MOSCOW, pages 94 *

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RU2174946C1 (ru) 2001-10-20

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