• 专利附录
  • 专利说明
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    • 专利摘要:
    Ethylene oxide is produced by contacting ethylene and oxygen in the presence of a chlorine containing reaction modifier with a silver containing catalyst, nitropropane being also present. The nitropropane raises the selectivity of the process.
    公开号:SU1468417A3
    申请号:SU853953990
    申请日:1985-09-11
    公开日:1989-03-23
    发明作者:Хейден Перси
    申请人:Империал Кемикал Индастриз Плс (Фирма)；
    IPC主号:
    专利说明:

    one
    The invention relates to the field of olefin oxides, in particular, to an improved method for producing ethylene oxide,
    Example 1. Porous carrier on the basis of og, α-alumina and impeccia surface area 0.5, pore volume 0.43 ml per 1 g, SiO content ,. equal to p, 38%, and the content of sodium 121 in the form of rings with an outer diameter of 7.8 mm, an inner diameter (hole) of 3.1 mm and a thickness of 7.8. diameters, is impregnated with a solution of silver nitrate dissolved in aqueous isopropylamine. Impregnated wet solid is subjected to pyrolysis by heating in a stream of nitrogen at. Temperature to. The product is cooked with hot water and dried. The dried catalyst is impregnated with an aqueous solution of potassium formate, the solution is drained. And the catalyst is dried. In the final form, the catalyst contains 16% by weight of silver and 500 1chp of added potassium.
    The catalyst was crushed and hydrogenated to obtain 112 g of a ground substance having a particle size in the range of 1-3.35 mm. It is loaded into a stainless steel reactor having an internal diameter of 10.8 mm and a length of 2.58 mm. Ethylene gas mixture
    -
    (30%) 5 oxygen (8%) carbon dioxide j (2 j5%) s vinyl chloride (12 ppm) ethyl chloride (O) and 2-nitropropane (20) with nitrogen up to 100% with nitrogen at an overpressure of 15 atm above the catalyst at a temperature of The pelvis is passed with a volume flow of 3070. The reaction yields ethylene oxide and carbon dioxide, the conversion of oxygen is 20%, and the selectivity of synthesis of ethylene oxide reaches 87% (i.e. 87 moles of ethylene oxide are formed from SO of moles of converted ethylene),
    PRI me R 2 Preparation of the catalyst.
    Metal silver particles uniformly cover catalysts ™ mash carrier pellets, consisting of porous, high-purity alumina, containing 250150 mpn of sulfur in terms of silicon, and 40 ± 10 million sodium compounds in terms of sodium, and 12 ± 3 ivmH potassium compounds in terms of potassium, and made in the form of cylinders with a diameter of 8 mm and a diameter of 8 mm with seven longitudinal holes passing through Ij22 mm, one of which passes through the center, and the rest are regularly spaced on, a circle with a diameter of 4.39 mm, the center of which is lies on the center axis of the okalesh. The average pore diameter of porous alumina is 2–3 µm, its porosity, estimated from water absorption data, is 0.3610.03 mg per 1 g, and the surface area is about 0.5 m / g
    Silver nitrate (4.418 g) was dissolved at 70 ° C in distilled water (896 mp) and the resulting solution was cooled to 50 ° C. Monoisopropyl amine (4800 ml) was added to this solution with stirring and cooling. They are slow enough to avoid an undesirable rise in temperature. The temperature is maintained in the range of 40-60 ° C, the resulting clear solution is cooled to room temperature.
    The pellets of the carrier (4200 g) were evacuated and a solution of silver nitrate-monoisopropylamine complex (5000 mp) was added. After contacting the solution for 30 minutes, it was impregnated.
    j j 15
    20 25 30
    40
    r d d - ekin SS
    The dryers are separated from the residual solution and allowed to drain. The pellets of the carrier, wet from the impregnated solution of the complex, are loaded into a perforated basket, which is then loaded into the reactor. The fed carrier is heated in a stream of hot atsoTa gas, the temperature initially being 100 ° C, and then it is gradually raised to 18 hours. The impregnated complex is decomposed leaving the chambers. silver, uniformly dispersed over the surface of porous oxides, spruce b-alumina. The pellets also contain a residue of substances containing carbon and nitrogen.
    The silver coated oxides are then contacted with hot air during the process, which begins by passing a stream of 5% air in nitrogen over pellets heated to 150 C. Then the air content in the gas stream and the temperature of the reactor gradually increase to 100% and 280 ° C. The rate of both changes is sufficiently slow to avoid uncontrolled increase in the temperature of the pellets due to the exothermicity of the process. Upon reaching 280 ° C, the pellets are in contact with an air stream for an additional 2 hours and then allowed to cool.
    The resulting silver-coated pellets, now substantially free from residues resulting from the decomposition of the silver nitrate-monoisopropylamine complex, are contacted with a stream of hot water in the temperature range of 90-100 ° C for 16 hours, then cooled, allowed to drain and dried by contacting with a stream of hot nitrogen at 150 s. The product is a catalyst precursor and can be characterized as a substantially pure, dry dispersion of silver particles uniformly deposited on the surfaces of both internal and Argular, porous oi-alumina.
    The catalyst precursor (4945 g) is impregnated with dripping by contacting at room temperature with 3323 ml of potassium formate solution in aqueous methanol. Aqueous methanol solvent contains 0.2%
    water of no volume and 17.9 g of potassium formate; Contacting is achieved by pumping potassium formate through the catalyst precursor pool, collecting the liquid and recycling it through the bed for 16 hours. After this impregnation step is completed, the catalyst pellets are left to drain the liquid and dried in a stream of warm nitrogen at 150 ° C. In the final form, the catalyst contains 500-600 million potassium.
    This preparative process is repeated to produce two additional catalyst batches. Three batches are mixed and tested. one
    The catalyst test is carried out
    in the following way. A tubular reactor with an internal diameter of 39 mm is loaded with a catapiser to produce a 10.7-meter spine layer (layer volume 12.8 l) and a three-meter section along the length of the tube above the catalyst is packed with fine inert alumina. The tube is surrounded with a liquid heat exchange medium for temperature control. At start-up, the composition of the gas fed to the reactor is as follows: n 6%; 27%; vinyl chloride 6 mpn; ethane 0.1%; 2-nitropropane 20 the rest is essentially methane with a small proportion of inert gases. Feed to the reactor was used at 75 ° C and a pressure of 18.5 atm with a gas hourly space velocity of 3600. The reactor temperature is then raised to initiate the reaction. At the same time, oxygen, ethylene, ethane, methane, 2-nitropropane, and vinyl chloride are mixed with recycle gas to obtain the required feed composition. After 26 days of operation of the unit, 1.03 MV4 oxygen is mixed with the recirculation gas; 1.4 ethylene; 6.8 l / h of ethane and 36 ml / h of vinyl chloride in methane, and everything is recalculated into vapors at standard pressure and standard temperature, plus a discontinuous methane flow, sufficient dp of pressure control in the installation, plus 2-nitropropane. The introduction of 2-nitropropane is carried out by pumping a liquid 2-nitropropane using a pressure micropump having a waste valve designed to operate at 30 atm. The temperature of 2-nitropropane in the pump is, at
    . 20
    25
    4Q
    near 20 ° C and it is substantially free from air, oxidizing agents, alkalis, acids and water. It is introduced at a process point, at which the temperature is, a pressure of 18 atm (abc.) At a flow rate of 3.7 ml / h of liquid to a stainless steel mesh, through which
    10 all process gas is passed through.
    The composition of the feed to the reactor according to the analysis data is as follows: 0 7.5%; CjH4 27%; WITH 0.3%,
    15 vinyl chloride 7.2 w; ethyl chloride 0.9 mpn; ethane 0.1%; 2-nitropropane 20 0.12% of water vapor, an estimate of about 3 mpp of nitrogen oxides; the rest is essentially methane. The analysis is performed at the reactor inlet and less nor less analysis error is provided as a result of water condensation than that observed when feeding N0 and N0 instead of 2-nitropropane. The reaction was charged at 18.5 atm and hourly space velocity of 3,600 hours. The oxygen conversion in the reactor was 28%. The reaction produces a selectivity of fy ethylene equal to 87%. The average catalyst temperature is 255 ° C. The gaseous product is cooled to 75 ° C before contacting with 250 l / h of water.
    35 at 20 ° C dp absorption of the product - ethylene oxide. The resulting gas stream is then divided, with a part in contact with 250 l / h of a 0.5% by weight solution of caustic soda in a carbon dioxide scrubber. Discharging the 1Y from the scrubber, the gaseous product and the bypass stream are combined and then compressed to produce a recycle gas stream.
    45 No solid deposits occur as a result of the reaction of nitropropane with ethylene (precipitation may occur under certain conditions between NO / NO and ethylene
    50 even at ambient temperature D1). No corrosion is observed in the make-up section of the reactor.
    Example 3. A catalyst similar to that shown in example 2, but containing 300-330 million potassium, is tested as follows. Tubular reactor with internal diameter
    55
    9 f-w is loaded with a catalyst, a catalyst semi-layer 10 m long (layer volume 11.92 l) and a pipe section 3 m long above the catalyst bed, filled with an inert linear clay deposits. The tube is surrounded by heat-exchanging fluid for temperature control. When starting up, the feed gas of the reactor has the following composition; Oh, 6%; C, 27% | vinyl chloride ethane, 2-nitropropane 41 mpn and the rest is substantially ethane with a small proportion of inert gases. The feed of the reactor is carried out at 75 ° C and an atm pressure of 3600 hourly space velocity. The temperature of the reactor is raised to initiate the reaction. Ethylene, ethane, methane, 2 nitropropane and vis-shchloride oxygen feeds are then mixed with recycle to produce the desired composition under-m-iTKK, 2-nitropropane. are introduced by pumping a liquid 2-nitropropane with a displacing micropump having a waste valve that operates at 30 atm. The temperature of the 2-nitropropane in the pump is approximately 20 ° C and it is substantially free from air, oxidizing agents, acids, and water. It is introduced at a process point, at which the temperature is 70 ° C, a pressure of 18 bar (abs.) At a flow rate of 4, .8 ml / h into a knitted stainless steel mesh, through which all the process gas is passed.
    After 14 days of operation, the reactor feed according to the analysis data has the following composition: 0 8.2%, 27%, CO 1% s vinyl chloride 5.9 ethylene oxide 0.8, ethane 0.17.2-nitropropane 32 million, Og 8 , 3 mn, N0 2.0 wn 0.12% of water vapor, and the rest is essentially methane. The analysis is carried out at the reactor inlet and revealing a smaller analysis error due to water condensation than that observed when applying N0 and N0 instead of 2-nitropropane. Recharge feeds are carried out at 75 ° C and 18.5 atm with an hourly rate of 3340 h, The conversion of oxygen in the reactor is 28%. The reaction yields a selectivity for the converted α-ethylene that is 84.2%. The average temperature of the catalyst. The gaseous product is cooled to 75 C ne
    By contacting with 250 l / h of water at 20 ° C to absorb the product, ethylene oxide, the resultant gas stream is then divided, with a part in contact with 250 l / h of 0.5 wt. with a solution of caustic salt in a carbon acid scrubber. The gaseous product released from the scrubber and the bypass stream are combined and then combined to produce a recycle gas stream. No solid deposits are observed as a result of the reaction of nitroprop-5 with ethylene (precipitation may occur under certain conditions between NO / NO and ethylene even at ambient temperatures). No corrosion is observed in the feed n section of the reactor installation.
    In the case of liquids and solids, ppm means parts by mass per million, and for gases, parts per million. Hourly 5 volumetric gas velocities are calculated: ana at 20 ° C and atmospheric pressure.
    PRI me R 4. Obtaining a catalyst
    Tablets carrier for the Q-catalyst, consisting of high-frequency porous C4-alumina with admixture of silicon oxide (250150 ppm) in terms of silicon, sodium compounds (U iOtlO) in terms of sodium and potassium compounds (12t3 million) in terms of potassium, cylindrical with a diameter of 8 mm and a length of 8 mm, penetrated by seven longitudinal atverses: mi-diameter of 1.22 mm, one of the jr. which are central, while the rest are evenly spaced around a diameter of 4.38 mm and centered on the axis of the tablet, evenly covered with metallic silver particles. The mean diameter of the scientific research institute. The pore diameter of porous oxide of pupine is 2-3 μm, the porosity determined by the absorption of water is 0.36 ± 0.03 mgg / g and the specific surface area
    0.5 MVr.
    Silver nitrate (4418 g) was dissolved in distilled water (896 ml) and the resulting solution was cooled to 50 ° C. With stirring and cooling, monoisopropylamine (4800 ml) is slowly added to the resulting solution. In order to avoid unnecessary.
    to increase the temperature, the addition of mines is carried out rather slowly, keeping the temperature in the range
    35
    40-60 C. The resulting prozacna solution is cooled to room temperature.
    The tablet carrier (4200 g) is evacuated and a solution of silver-mono-isopropylamine nitrate complex (5000 ml) is added to it. After contacting the solution for 30 minutes, the impregnated tablets are separated from the remaining solution and dried.
    The preformed carrier wet from the impregnating solution of the complex is placed in a perforated basket, which is loaded into the reactor. The impregnated carrier is heated in a stream of heated nitrogen gas at an initial temperature of 100 ° C, which is then gradually increased over 18 hours to 240 ° C. The impregnating complex decomposes with uniformly distributed silver particles on the surface of a tablet of porous oi-alumina. Tablets also contain compound residues.
    carbon and nitrogen.
    Silver-coated tablets are then contacted with hot air, and first they pass a stream of nitrogen with 5% air over the tablets heated to 150 ° C. Then, the air content in the gas stream is gradually increased to 00% with a gradual increase in temperature to 280 C. The rate of change of both parameters is sufficiently low in order to avoid coherent heating of the tablets due to the thermal process. After the temperature reaches 280 ° C, the tablets are in contact with the air flow for another 2 hours, after which it is cooled.
    The resulting silver-coated tablets, essentially not containing
    The residues of the decomposition products of the Comp.exa silver-monoisopropyl-amine nitrate are contacted with a stream of hot water in the temperature range of 90-100 ° C for 16 hours, then cooled, the excess WATER is drained and dried by contacting with a stream of hot nitrogen at 150 ° C. The resulting product is a catalyst precursor and is characterized as a clean, dry dispersion of silver particles, uniformly covering both the outer and the inner surface of C16-POTS aluminum porous tablets.
    The catalyst precursor (A945 g) is impregnated with potassium by contacting at room temperature with 3323 ml of a solution of potassium forma in methanol. The single-methane aII solution contains 0.4% by volume of water and 25.4 g of potassium format. The contacting is carried out by pumping the potassium format solution through the precursor catalyst layer, collecting the solution and resizing it for 6 hours. After this impregnation stage is completed, excess water is removed and dried in a stream of heated nitrogen at 150 ° C. The resulting catalyst contains 750 potassium.
    The preparation of the catalyst is repeated to obtain two additional lots of catalyst. Three batches of catalyst are used. The catalyst test is carried out as follows. A tubular reactor with an internal diameter of 39 mm locks the catalyst in a layer with a length of 10.7 liters (bed volume is 12.8 liters) and a tableted inert alumina is placed over the length of the reactor in 3 meters. For reg1, the temperature is broadened and the reactor is surrounded by heat exchanging liquid. In the initial period, the composition of the gas mixture fed to the reactor includes: 0 6%; , 27%} chloride. Vinyl 6 million; h — 0.1%; 2-nitrogfopana 20 million, and the rest of the mixture along with:, the methane forms with a small amount of inert gases. The gas supply to the reactor is carried out at 75 ° C, a pressure of 18.5 atm and a gas hourly space velocity of 3,600 hours. For initiating the reaction, the temperature of the reactor is increased. Oxygen, ethylene, ethane methane, 2-nitropropane, and vinyl chloride, which are supplied as feedstock, are then mixed with recycle gas to produce the desired gas mixture. After 142 days, 1.03 of oxygen, 1.4 m / h of ethylene, 6.8 l / h of ethane and 36 ml / h of vinyl chloride (for all components in the vapor phase at normal temperature and pressure) plus periodically fed are mixed with recycled gas. a flow of methane in an amount sufficient to control the pressure in the installation plus 2-nitropropane. 2-Nitropropane is fed by injecting liquid 2-nitropropane
    using an injection piston micropump equipped with a safety valve system operating under a pressure of 30 atm. The temperature of 2-nitropropane in the pump is about 2-nitropropane and in fact does not contain air, oxidizing agents, alkalis, acids, and water. 2-Nitropropane is introduced into the process at a point with a temperature Q and a pressure of 18 atm (absolute) with a flow rate of liquid
    7MP through a stainless stapled mesh, through which all gaseous components are also fed. 15
    According to the analysis, the mixture supplied to the reactor contains: Oj 8.2%, 27% 5 CO lsl%, vinyl chloride 752 ethyl chloride 0.9 million, stage 05l% 5 2-nitropropane 38 mnp, 20 water vapor 0.12% and set the amount of nitrogen oxides is about 3 ppm and the remainder of the mixture is essentially converted to methane. The analysis is carried out at the entrance to the reactor and a small inaccuracy of the analysis occurs due to the condensation of water, and not then when CO and NO are introduced instead of 2-nitropropane. Raw materials are fed into the reaction at 75 ° C, a pressure of 18.5 atm o and a volumetric hourly rate of 3700 h. The conversion of oxygen during the passage through the reactor is 29%. The selectivity of the conversion of ethylene in the reaction of 80.3%. The average temperature of the catalyst. The gases formed before contacting at 20 ° C with water (250 l / h) in order to extract the ethylene oxide are cooled to 7 5 ° C. The resulting gas stream is then separated and made one year.
    the part is contacted in a scrubber for carbon dioxide with a 5% (May / May.) solution of sodium hydroxide (250 l / h). The washed gaseous product and the bypass gas stream are combined and compressed to form a recycle gas stream. In the reaction of nitropropane with ethylene, no solid deposition occurs (precipitates can occur at certain NO / NO and ethylene ratios even at room temperature)
    8 sections of the plant, where the reaction raw materials are supplied, no corrosion is observed,
    EXAMPLE 5 A catalyst, analogous to the catalyst of Example 2, but containing 180–200 million potassium, is tested in the following manner, B 50
    55
    Q
    five
    0 5 o.,
    with
    0
    five
    A 39 mm diameter reactor was loaded with a catalyst layer 10 m in length (layer volume 11.92 l) and an inert tableted alumina layer 3 m long was placed above the catalyst layer. The temperature was controlled by a heat exchanging fluid to control the temperature. At the initial stage, a gas mixture consisting of: Oj 6%; 27%; vinyl chloride 6 ethane 0.1%, 2-nitropropane 41 million, and the rest of the mixture forms methane with a small amount of inert gases. The feed to the reactor is carried out at 18.5 atm and with a volumetric flow rate of the gas mixture of 3,600 4 To initiate the reaction, the temperature of the reactor is then increased. To obtain the desired composition of the mixture, oxygen, ethylene, ethane, methane, 2-nitropropane, and vinyl chloride are then mixed with recycle gas. 2-Nitropropane is fed by means of a reciprocating piston micropump with a safety valve that withstands a pressure of 30 atm. The temperature of 2-nitropropane in the pump is approximately 2-nitropropane, which essentially does not contain air, oxidizers, alkalis, acids, and water. 2-nitropropane is introduced at a point with a temperature of 70 ° C, an absolute pressure of 18 atm, at a feed rate of 1.2 ml / h through a tied stainless steel mesh, through which also the gas feed is also supplied.
    After four days of operation, the feedstock fed to the reactor according to the analysis contains: 0 8.2%; 27%; 0.5%; - vinyl chloride 2 ethylene chloride 0.4 ethane 0.1%; 2-nitropropna 8 million; N0 2 N0 1 water vapor 0.12%, and the rest of the mixture actually forms methane. The analysis is carried out at the inlet to the reactor and less accurate analysis occurs due to condensation of water, and not when, instead of 2-nitropropane, N0 H..NO is introduced. Raw materials in the reaction served when. 18.5 atm and volumetric gas velocity per hour 3500 Oxygen conversion when passing through the reactor 22%. The selectivity of the conversion of ethylene in the reaction of 83.2%. Average temperature catalyst. Formed gases before contacting with water (250 l / h) to remove
    the formation of ethylene oxide gives up to. The resulting gas stream is then separated and part of it is contacted in a carbon dioxide scrubber with a 5% (w / w) sodium hydroxide solution (250 l / h). The scrubber-treated gaseous product and bypass stream are combined and then compressed to produce a recirculated gas stream. The formation of solid deposits as a result of the reaction of cytopropane with ethylene is not observed (deposits may form under certain conditions in the reaction between NO / NOj, with ethylene even at room temperature). In the installation section, where raw materials are supplied, no corrosion is noted.
    Values in the case of liquids or solids mean parts per million by weight, and in the case of gases, parts per million by volume. Volumetric hourly gas scrims were calculated at atmospheric pressure.
    EXAMPLE 6 The tests are carried out similarly to the test with the steel tube BAM 50/60, and the tube is additionally equipped with a heating device
    ACTIVITY, LET YOU WRITE OClT e STEEL
    heating to a temperature of 80 ° C, which is being tested.
    The tests are carried out with nitromethane and 2-nitropropane at 80 ° C, i.e. at a lower temperature than the one at which ethylene oxide is produced. However, it is higher than the temperature at which the injection pump is operating. This temperature allows
    estimate the limits of safe process conditions.
    In all experiments, a tube made of soft steel with a depth of 69 cm with an outer diameter of 60.5 and an inner diameter of 52.3 mm was used, i.e. with a st. na thickness of 4.1 mm. At one end, the tube was welded with a 10 mm thick Yul soft steel plate with a thickness of 6.5 mm. Its other end remained open.
    On the outer surface of the tube, along its entire length, a heating coil is wound, to which a current from the adjusting transformer is supplied via a long cable. Dp control
    heating rates in the circuit include an ammeter. Dp prevent the loss of heat the tube is covered with insulating material.

    0 5
    ABOUT
    with Q
    5 n
    five
    During heating, the tube is placed vertically5 supported by a steel plate on a lead plate 25 mm thick, which is placed on a large steel plate.
    Through the top end, the open end of the pipes pass the fuse and the thermocouple. The fuse is positioned in such a way that the level of the liquid is approximately 2 cm from the top of the tube, and the pap itself is immersed in a liquid for 3-4 cm. In this position, the fuse is retained using a cage made of thin steel wire ..
    The thermocouple is passed through the fuse, and the wall of the pipe is lowered into the liquid to a depth of 10 cm, i.e. it is located 6 cm below the fuse. The signal from the thermocouple (a relatively cold spa that was in a mixture of WATER and ice at) is recorded at a safe distance from the point of ignition.
    Pentholitol (a mixture of pentaerythritol tetranitrate and trinitroluol) weighing 56 g, diameter 31 mm and 52 mm long, with a notch for a detonator at one end with a depth of 19 mm, is used as a fuse. The ignition ignition is carried out using an electric detonator with a diameter of 7.
    To protect the fuse from the actual liquid in the process of testing it, before wrapping it in a tube, it is wrapped with a layer of thick plastic.
    Preliminary testing.
    The tube is wrapped around with a layer of fiberglass thermal insulator and placed on a lead plate; located on a large steel plate. The heating coil is connected to the power cable 7g and the whole structure is fixed with sandbags, placed around to the height of the upper end of the tube.
    The test liquid is poured into the tube B to the desired height, carefully lowered into it, the fuse and secured it with a wire.
    The thermocouple is placed in the liquid to the desired depth and secured.
    A detonator is inserted into the igniter and connected to the ignition cable.
    Using a controlled power source, the temperature of the liquid, at a rate of 4 C / s, is raised to and maintained at this temperature for about 5 minutes.
    for uniform heating of the fluid throughout the volume.
    After that, the detonator-ignition system is ignited. Results: a loud explosion, the tube breaks into pieces along the entire length9 in the steel base section and the lead plate as a result of the explosion, holes are punched
    Thus, the entire sample detonates.
    2-Nitropropane - weak explosion (only fuse).
    A large portion of the insulated tube remains intact; some amount of 2-nitropropane remains inside the tube; the top of the tube is folded back by the explosion of the fuse. So 2-nitropropane does not detonate,
    Under the test conditions, nitromethane is detonated, 2-nitropropane does not detonate under these conditions.
    On the basis of the test conducted by the Institute, it can be concluded that since nitropropane does not detonate with a weak explosion, the fuse at those temperatures at which the process is actually carried out, it can be used for the safe conduct of this process with the adoption of appropriate safety measures. Strong explosion in experience
    with nitromethane, suggests that use of this compound is associated with significant risk. Thus, the proposed method allows to increase the safety of the process while increasing the oxygen conversion.
    权利要求:
    Claims (1)
    [1]
    Invention Formula
    1, A method for producing ethylene oxide by oxidizing ethylene with oxygen in the presence of a chlorine-containing modifier and a silver-containing catapystat at 215-265 ° C, characterized in that, in order to increase the safety of the process, the oxidation is carried out in the presence of nitropropane,
    2, The method according to claim 1, distinguishes between a and u. the fact that nitropropane is served in the form of a liquid with a displacement pump equipped with a relief valve operating at a pressure of 30 atm,
    3, the method according to claim 1, characterized in that the nitropropane is introduced at the point at which the temperature is and the pressure is 18 atm
    4, The method of claim 1, I, is different from the fact that nitropropane is introduced through a stainless steel mesh.
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    同族专利:
    公开号 | 公开日
    EP0176253A1|1986-04-02|
    AU588249B2|1989-09-14|
    GB8423044D0|1984-10-17|
    DE3576504D1|1990-04-19|
    JPS6176469A|1986-04-18|
    US4822900A|1989-04-18|
    EP0176253B1|1990-03-14|
    JPH066582B2|1994-01-26|
    CA1236472A|1988-05-10|
    AU4704385A|1986-03-20|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    GB848423044A|GB8423044D0|1984-09-12|1984-09-12|Production of ethylene oxide|
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