EP2961691A1 - Procédé de synthèse d'acide prussique à partir d'un réacteur secondaire de conditionnement de formamide - Google Patents

Procédé de synthèse d'acide prussique à partir d'un réacteur secondaire de conditionnement de formamide

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Publication number
EP2961691A1
EP2961691A1 EP14707388.6A EP14707388A EP2961691A1 EP 2961691 A1 EP2961691 A1 EP 2961691A1 EP 14707388 A EP14707388 A EP 14707388A EP 2961691 A1 EP2961691 A1 EP 2961691A1
Authority
EP
European Patent Office
Prior art keywords
formamide
reactor
mbar
steel
bar
Prior art date
Legal status (The legal status 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 status listed.)
Withdrawn
Application number
EP14707388.6A
Other languages
German (de)
English (en)
Inventor
Ralf Böhling
Michael Schipper
Jens Bernnat
Wilhelm Weber
Peter Petersen
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
BASF SE
Original Assignee
BASF SE
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 BASF SE filed Critical BASF SE
Priority to EP14707388.6A priority Critical patent/EP2961691A1/fr
Publication of EP2961691A1 publication Critical patent/EP2961691A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C3/00—Cyanogen; Compounds thereof
    • C01C3/02—Preparation, separation or purification of hydrogen cyanide
    • C01C3/0204—Preparation, separation or purification of hydrogen cyanide from formamide or from ammonium formate
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/30—Loose or shaped packing elements, e.g. Raschig rings or Berl saddles, for pouring into the apparatus for mass or heat transfer
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/32—Packing elements in the form of grids or built-up elements for forming a unit or module inside the apparatus for mass or heat transfer
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/30—Details relating to random packing elements
    • B01J2219/302—Basic shape of the elements
    • B01J2219/30215—Toroid or ring
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/30—Details relating to random packing elements
    • B01J2219/304—Composition or microstructure of the elements
    • B01J2219/30408—Metal
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/30—Details relating to random packing elements
    • B01J2219/304—Composition or microstructure of the elements
    • B01J2219/30416—Ceramic
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/30—Details relating to random packing elements
    • B01J2219/304—Composition or microstructure of the elements
    • B01J2219/30475—Composition or microstructure of the elements comprising catalytically active material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
    • B01J2219/322—Basic shape of the elements
    • B01J2219/32203—Sheets
    • B01J2219/32237—Sheets comprising apertures or perforations
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
    • B01J2219/324—Composition or microstructure of the elements
    • B01J2219/32408—Metal
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
    • B01J2219/324—Composition or microstructure of the elements
    • B01J2219/32466—Composition or microstructure of the elements comprising catalytically active material

Definitions

  • the present invention relates to a process for the preparation of hydrogen cyanide by catalytic dehydration of gaseous formamide in at least one main reactor and a downstream post-reactor and the use of a post-reactor in a process for the production of hydrogen cyanide by catalytic dehydration of gaseous formamide.
  • Hydrocyanic acid is an important basic chemical used as a starting material in, for example, numerous organic syntheses, such as the production of adiponitrile, methacrylic acid esters, methionine and complexing agents (NTA, EDTA).
  • organic syntheses such as the production of adiponitrile, methacrylic acid esters, methionine and complexing agents (NTA, EDTA).
  • NTA methacrylic acid esters
  • EDTA complexing agents
  • alkali cyanides used in the mining and metallurgical industries.
  • Ammonia is washed out with sulfuric acid from the raw gas. Due to the high selectivity, however, only very little ammonium sulfate is produced.
  • the ammonia formed catalyzes the polymerization of the desired hydrocyanic acid and thus leads to an impairment of the quality of the hydrocyanic acid and a reduction in the yield of the desired hydrocyanic acid.
  • the polymerization of hydrocyanic acid and the associated soot formation can be suppressed by the addition of small amounts of oxygen in the form of air, as disclosed in EP-A-0 209 039.
  • EP-A-0 209 039 discloses a process for the thermolytic cleavage of formamide on highly sintered alumina or alumina-silica moldings or on high-temperature corrosion-resistant chromium-nickel-stainless steel moldings. According to the examples in EP-A-0 209 039, conversions of 97.5% to 98.6% and selectivities of 94.8% to 96.7% are achieved.
  • the prior art discloses further processes for the production of hydrogen cyanide by catalytic dehydration of formamide.
  • WO 2004/050582 relates to a process for the preparation of hydrocyanic acid by catalytic dehydration of gaseous formamide, in a reactor having an inner reactor surface made of a steel containing iron and chromium and nickel, wherein the reactor preferably contains no additional internals and / or catalysts ,
  • the selectivity of blue acids is between 90 and 98.5% and formamide conversions between 70 and 97%.
  • WO 2006/027176 a process for the production of hydrogen cyanide by catalytic dehydration of gaseous formamide is disclosed in which from the product mixture upon dehydration a formamide-receiving reflux is recovered and recycled to the dehydration, wherein the formamide-containing recycle stream 5 to 50 wt. - contains% water.
  • the process generally achieves a formamide conversion of 80 to 98%, based on the total amount of formamide added to the dehydration, and the selectivity of hydrocyanic acid formation is generally 85 to 96%.
  • US 2,042,451 relates to a process for the catalytic dehydration of formamide for the production of hydrogen cyanide.
  • the catalyst used is a heated surface (brass or iron), which is coated by a thin catalytically active oxide layer of zinc, manganese, aluminum, chromium or tin oxide. According to the examples, the method according to
  • DE-A-1 209 561 discloses a process for the production of hydrocyanic acid from formamide in which ferric oxide is used as a catalyst obtained by partial or complete binding to acids to form salts or by combination with one or more non-volatile oxides of 1 - Disabled to 6-valent metals.
  • the catalysts are in pelleted form or as extruder-shaped catalyst grains. According to
  • DE-A-1 209 561 has a regenerated catalyst comprising the above-mentioned catalyst components, a higher activity than the freshly used catalyst.
  • the maximum yield of hydrocyanic acid is 94% according to the example given in DE-A-1 209 561.
  • DE-A-1 000 796 relates to a process for the cleavage of formamide vapor for the production of hydrogen cyanide, wherein a temperature gradient within the furnaces for cleavage is taken into account by the fact that the cleavage on lumpy or granular combingebrannten, senoxid ambiencen silicates or spinels in a cleavage space is made, the wall of which has a lower catalytic activity than that of the catalyst in the cleavage space, said wall consists for example of stainless steel.
  • DE-A-477 437 discloses a process for the catalytic production of hydrocyanic acid from formamide in which formamide vapors are passed in considerable dilution at high speed at temperatures above 300 ° C using metal tubes in the absence of dehydrating catalysts over metals as catalysts , Suitable metals are V2A steel, nickel and aluminum. According to DE-A-477 437, it is already sufficient to produce the wall of the reaction vessel from the effective metal or to line it with this. With the method disclosed in DE-A-477 437 yields of hydrocyanic acid of 90 to 98% are achieved according to the examples.
  • hydrocyanic acid can be obtained in high selectivities of generally> 90% and good conversions of generally> 90% in accordance with the abovementioned process.
  • the object of the present application over the prior art is therefore to provide a process for the catalytic dehydration of formamide for the production of hydrocyanic acid, which can be operated with the highest possible conversion of formamide, preferably with full formamide conversion, and wherein the abovementioned Disadvantages are avoided.
  • This object is achieved by a process for producing hydrogen cyanide by catalytic dehydration of gaseous formamide, comprising the steps
  • FIG. 1 shows the formamide residual content in the exhaust gas in% by volume (y-axis) as a function of the temperature in ° C. (x-axis) at full conversion with respect to the equilibrium conversion.
  • y-axis the formamide residual content in the exhaust gas in% by volume
  • the high formamide conversion can be achieved with good selectivities of hydrocyanic acid of> 88%, preferably> 90%, particularly preferably> 93%.
  • the procedure according to the invention makes it possible to dispense with condensation with high-boiling-point formation and re-distillation of unreacted formamide, and the hot reaction gas can be quenched directly, usually in the ammonia absorber. Problems that Usually occur by polymer deposits in the formamide capacitors, can also be avoided.
  • adiabat is to be understood as meaning that the system, that is to say the reaction mixture in the secondary reactor, is converted (heat-sealed) without exchanging thermal energy with its surroundings.
  • step (i) of the process according to the invention the catalytic dehydration of gaseous formamide in at least one main reactor to an intermediate gaseous reaction product, wherein the conversion of formamide at the output of the main reactor is at least 95%, based on the formamide used.
  • the catalytic dehydration in step (i) can in principle be carried out by all methods known to the person skilled in the art, the conversion of the formamide at the outlet of the main reactor having to be at least 95%, based on the formamide used.
  • the reactor used in step (i) of the process according to the invention may be any of those known to the person skilled in the art for the dehydration of formamide.
  • the inner surface of the reactor used for dehydration may serve as a catalyst for dehydration of formamide. Therefore, an iron-containing surface is preferably used as the inner surface of the reactor.
  • the inner surface of the reactor is constructed of steel.
  • the steel contains iron as well as chromium and nickel.
  • the proportion of iron in the steel which most preferably forms the inner reactor surface is generally> 50% by weight, preferably> 60% by weight, more preferably> 70% by weight.
  • the remainder are generally nickel and chromium, where appropriate, small amounts of other metals, such as molybdenum, manganese, silicon, aluminum, titanium, tungsten, cobalt in a proportion of generally 0 to 5 wt .-%, preferably 0.1 to 2 Wt .-% may be included.
  • Suitable steel qualities for the inner reactor surface are generally steel grades according to standards 1 .4541, 1.4571, 1 .4573, 1.4580, 1.4401, 1 .4404, 1.4435, 2.4816, 1 .3401, 1.4876 and 1.4828.
  • step (i) of the process according to the invention it is likewise possible for the catalytic dehydration in step (i) of the process according to the invention to be carried out in addition to the catalytically active inner reactor surface or catalysts instead of a catalytically active inner reactor surface in the presence of shaped bodies.
  • the moldings are preferably highly sintered moldings, composed of aluminum oxide and optionally silicon oxide, preferably from 50 to 100% by weight of aluminum oxide and 0 to 50% by weight of silicon oxide, particularly preferably from 85 to 95% by weight of aluminum oxide and 5 to 15% by weight % Of silica, or of chromium-nickel stainless steel, as described in EP-A 0 209 039.
  • suitable catalysts used in step (i) of the process according to the invention can be packings of steel or iron oxide from porous support materials, eg. As alumina, act. Suitable packs are for. As described in DE-A 101 38 553.
  • moldings are used, then it is possible to use both ordered and unordered moldings as possible moldings, for example by molding.
  • the size or geometry of the moldings used generally depends on the inner diameter of the reactors to be filled with these moldings, preferably tubular reactors.
  • the main reactor used in step (i) of the process according to the invention preferably a tubular reactor, more preferably a multitubular reactor, can comprise steel or iron oxide packings as catalysts, which are generally ordered packings.
  • the ordered packs are static mixers.
  • the static mixers may be of any geometry known to those skilled in the art.
  • Preferred static mixers are constructed from sheets, which may be perforated sheets and / or shaped sheets. Of course, also shaped perforated plates can be used. Suitable static mixers are z. As described in DE-A 101 38 553.
  • the catalytic dehydration in step (i) of the method according to the invention thus in the presence of moldings selected from highly sintered shaped bodies, composed of alumina and optionally silica and chromium-nickel-stainless steel moldings, or in the presence of packs made of steel or Iron oxide on porous support materials, or in the presence of ordered packings of steel carried out as catalysts, and / or the inner reactor surface of the main reactor is constructed of steel and serves as a catalyst.
  • the catalytic dehydration in step (i) of the process according to the invention is carried out at a temperature of from 350 to 700.degree. C., preferably from 400 to 650.degree. preferably 500 to 600 ° C, carried out. If higher temperatures are selected, deteriorated selectivities are to be expected.
  • the pressure in step (i) of the process according to the invention is generally from 70 mbar to 5 bar, preferably from 100 mbar to 4 bar, more preferably from 300 mbar to 3 bar, very preferably from 600 mbar to 1.5 bar absolute pressure.
  • the catalytic dehydration is preferably carried out in step (i) of the process according to the invention in the presence of oxygen, preferably air-oxygen.
  • oxygen preferably air-oxygen.
  • the amounts of oxygen, preferably air-oxygen are generally> 0 to 10 mol%, based on the amount of formamide used, preferably 0.1 to 9 mol%, particularly preferably 0.5 to 3 mol%.
  • the optimum residence time of the formamide gas stream in step (i) of the process according to the invention results in the preferred use of a tubular reactor as the main reactor from the area-specific formamide load, which is generally 0.1 to 100 kg / m 2 , preferably 2 to 50 kg / m 2 , particularly preferably 4 to 30 kg / m 2 , based on the tube inner surface of the tube or the multi-tube reactor.
  • the dehydration preferably takes place in the area of laminar flow.
  • the heating of the main reactor used in step (i) of the process according to the invention is generally carried out with hot burner exhaust gases (rolling gas) or by means of molten salt.
  • the resulting residual gas from the hydrocyanic acid synthesis can additionally be used. This generally contains CO, H2, N2, as well as small amounts of hydrogen cyanide.
  • step (i) of the process according to the invention is carried out up to a formamide conversion of at least 95%, based on the formamide used.
  • the selectivity to hydrocyanic acid is generally> 85%, preferably> 90%.
  • step (i) of the process according to the invention is introduced into an after-reactor at an inlet temperature of 350 ° C. to 700 ° C. (step (ii) of the process according to the invention).
  • Step (ii) of the process according to the invention relates to the introduction of the intermediate gaseous reaction product into a post-reactor having an inlet temperature of 350 ° C. to 700 ° C., wherein the post-reactor contains internals or beds of steel and is operated adiabatically. Built-ins are, for example, ordered packs.
  • step (ii) of the process according to the invention it is possible to increase the formamide conversion in the processes for the catalytic dehydration of gaseous formamide to equilibrium conversion (full conversion).
  • the equilibrium in the dehydration of formamide is temperature dependent.
  • At the stated inlet temperatures of 450 to 700 ° C formamide conversions of> 98% of the equilibrium conversion (full formamide conversion) are achieved, preferably of> 99%, more preferably of> 99.5%.
  • the postreactor has internals, e.g. ordered packings, or heaps of steel and is operated adiabatically.
  • the internals made of steel in the secondary reactor are preferably ordered packings, more preferably static mixers.
  • the static mixers are constructed from sheets, preferably perforated sheets and / or shaped sheets, wherein the perforated sheets can also be shaped perforated sheets.
  • Suitable static mixers are z. As described in DE-A 101 38 553.
  • the steel is present in the above-mentioned beds or internals, e.g. ordered packs, preferably static mixers, preferably static mixers made of sheets, of the secondary reactor selected from steel grades according to the standards 1 .4541, 1.4571, 1.4573, 1 .4580, 1.4401,
  • the post-reactor is operated in step (ii) of the process according to the invention at the same pressure as the main reactor, or at the pressure loss in the main reactor reduced pressure.
  • the outlet pressure of the gaseous, intermediate reaction product obtained in step (i) from the main reactor and the inlet pressure of the gaseous, intermediate reaction product obtained in step (i) into the postreactor in step (ii) each of the method according to the invention are identical.
  • the pressure in the postreactor in step (ii) is generally 70 mbar to 5 bar, preferably 100 mbar to 4 bar, more preferably 300 mbar to 3 bar, most preferably 600 mbar to 1, 5 bar absolute pressure.
  • the temperature in the post-reactor in step (ii) is generally 350 to 700 ° C, preferably 400 to 650 ° C, particularly preferably 500 to 600 ° C.
  • oxygen preferably air / oxygen
  • oxygen can serve to increase the catalytic activity of the catalytic material used in the post-reactor.
  • the hydrocyanic selectivity which can be achieved with the aid of the postreactor in step (ii) of the process according to the invention is generally from 70 to 100%, preferably from 90 to 100%, particularly preferably from 93 to 100%.
  • the gaseous formamide used in the process according to the invention in step (i) is obtained by evaporation of liquid formamide.
  • Suitable processes for vaporizing liquid formamide are known to those skilled in the art and described in the state of the art mentioned in the introduction to the description.
  • the evaporation of the formamide is carried out at a temperature of 1 10 to 270 ° C.
  • the evaporation of the liquid formamide in an evaporator at temperatures of 140 to 250 ° C, more preferably 200 to 230 ° C.
  • the evaporation of the formamide is generally carried out at a pressure of 20 mbar to 3 bar.
  • the evaporation of the liquid formamide is carried out at 80 mbar to 2 bar, more preferably 600 mbar to 1, 3 bar absolute pressure.
  • the evaporation of the liquid formamide is carried out at short residence times.
  • Very particularly preferred residence times are ⁇ 20 s, preferably ⁇ 10 s, in each case based on the liquid formamide.
  • the formamide can be evaporated almost completely without by-product formation.
  • the abovementioned short residence times of the formamide in the evaporator are preferably achieved in milli or microstructured apparatuses.
  • Suitable milli- or microstructured apparatuses which can be used as evaporators are, for.
  • Another process for the evaporation of liquid formamide and a suitable microvaporiser are described in WO 2009/062897.
  • the gaseous formamide used in step (i) is thus obtained by evaporation of liquid formamide at temperatures of 100 to 300 ° C., wherein a milli-or microstructured apparatus is used as the evaporator. Suitable milli-or microstructured apparatus are described in the aforementioned documents.
  • the inventive method has the advantage that a high formamide conversion, preferably full conversion in relation to the equilibrium conversion of formamide, is achieved. Therefore, in general, condensation with high boiler formation and re-distillation of unreacted formamide can be dispensed with, and the hot reaction gas leaving the secondary reactor can be quenched directly in the Nh absorber.
  • the quenching of the hot, the post-reactor leaving hydrocyanic gas-containing, tubular gas stream using dilute acid, preferably using dilute F SC solution is usually pumped in the circulation via a quench column. Suitable quench columns are known to the person skilled in the art.
  • the resulting NH3 is bound to ammonium sulfate.
  • the heat gas cooling, neutralization and dilution
  • a heat exchanger usually cooling water
  • At quenching temperatures of generally 50 to 560 ° C water is condensed out at the same time, which is discharged as a dilute ammonium sulfate solution generally through the bottom and disposed of.
  • hydrocyanic acid dissolved in the sump can be removed.
  • the bottom product can be such.
  • the quench column leaves an approximately 70 to 99% hydrocyanic acid gas stream. It may also contain CO, CO2, water and H2.
  • Optional Compressor It is possible for the quench column to follow a compressor which compresses the gas leaving the quench column overhead to a pressure corresponding to a desired process for further processing the hydrocyanic acid gas stream.
  • this method for further processing may be, for. B. be a workup to pure hydrocyanic acid or any other reactions of the hydrocyanic gas stream.
  • Another object of the present invention is therefore the use of a post-reactor in a process for the production of hydrogen cyanide by catalytic dehydration of gaseous formamide, wherein the post-reactor internals, for. B. contains ordered packings or beds of steel and is operated adiabatically.
  • Table 1 The measurements shown in Table 1 are carried out in a roller gas-heated Rohrbündelre- actuator with 1, 4 m long reaction tubes of 1 .4541 steel.
  • the information relates to a pipe.
  • the reactor is followed by a 1 m long post-reactor.
  • the secondary reactor is equipped with a sheet-metal packing with a surface-to-volume ratio of 250 m 2 / m 3 (MONTZ-Pak type B1 -250.60 material 1.4541, material thickness: 1 mm).
  • the reactor is operated at an empty pipe speed of 9.4 m / s.
  • the detailed conditions are given in the following table.

Abstract

L'invention concerne un procédé de production d'acide prussique par déshydratation catalytique d'un formamide gazeux dans au moins un réacteur principal et dans un réacteur secondaire situé en aval. L'invention concerne également l'utilisation d'un réacteur secondaire dans un procédé de production d'acide prussique par déshydratation catalytique d'un formamide gazeux.
EP14707388.6A 2013-03-01 2014-02-28 Procédé de synthèse d'acide prussique à partir d'un réacteur secondaire de conditionnement de formamide Withdrawn EP2961691A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP14707388.6A EP2961691A1 (fr) 2013-03-01 2014-02-28 Procédé de synthèse d'acide prussique à partir d'un réacteur secondaire de conditionnement de formamide

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
US201361771100P 2013-03-01 2013-03-01
EP13157414 2013-03-01
PCT/EP2014/053936 WO2014131883A1 (fr) 2013-03-01 2014-02-28 Procédé de synthèse d'acide prussique à partir d'un réacteur secondaire de conditionnement de formamide
EP14707388.6A EP2961691A1 (fr) 2013-03-01 2014-02-28 Procédé de synthèse d'acide prussique à partir d'un réacteur secondaire de conditionnement de formamide

Publications (1)

Publication Number Publication Date
EP2961691A1 true EP2961691A1 (fr) 2016-01-06

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EP14707388.6A Withdrawn EP2961691A1 (fr) 2013-03-01 2014-02-28 Procédé de synthèse d'acide prussique à partir d'un réacteur secondaire de conditionnement de formamide

Country Status (5)

Country Link
US (1) US20160009565A1 (fr)
EP (1) EP2961691A1 (fr)
JP (1) JP2016508481A (fr)
CN (1) CN105164051A (fr)
WO (1) WO2014131883A1 (fr)

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DE102005032541A1 (de) * 2005-07-12 2007-01-18 Basf Ag Verfahren zur Hydrierung von aldehydhaltigen Stoffströmen
WO2009056470A1 (fr) * 2007-10-29 2009-05-07 Basf Se Procédé amélioré pour produire de l'acide cyanhydrique
US20100284889A1 (en) * 2007-11-13 2010-11-11 Basf Se Method for producing hydrocyanic acid by catalytic dehydration of gaseous formamide
AU2008323040A1 (en) * 2007-11-13 2009-05-22 Basf Se Improved method for the production of hydrocyanic acid by means of catalytic dehydration of gaseous formamide
WO2011089209A2 (fr) * 2010-01-22 2011-07-28 Basf Se Évaporateur à chambre unique et son utilisation pour la synthèse chimique

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WO2014131883A1 (fr) 2014-09-04
CN105164051A (zh) 2015-12-16
JP2016508481A (ja) 2016-03-22
US20160009565A1 (en) 2016-01-14

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