SU798031A1 - Method of producing ammonia and methanol - Google Patents

Description

(54) METHOD OF OBTAINING AMMONIA AND METHANOL

residual methanol (about 1-2%) is heated to, mixed with water vapor and directed to medium-temperature conversion of carbon monoxide, as a result of which the gas is heated to, then the gases are cooled in a heat exchanger to 240 ° C and sent to low-temperature conversion carbon monoxide, where they are heated to. After cooling the converted gases, they are purified from carbon dioxide, methanated, compressed to 150 atm and sent to the ammonia synthesis cycle 21.

However, the technological sequence of processes envisaged in the known method necessitates the need for repeated cooling and heating of the process gas streams, which, firstly, complicates the method, and secondly, increases the heat loss when the gases are cooled with circulating water or air and causes additional consumption of process steam for carrying out processes such as methanol sieve and conversion of carbon monoxide.

The purpose of the invention is to simplify the method.

This goal is achieved by the fact that ammonia and methanol are produced by a method involving the conversion of hydrocarbons with water vapor on a nickel catalyst at a pressure of 40–70 at and a temperature of 700–900 ° C;

. hydrogen diffusion method from the converted gas, the conversion of carbon monoxide at 400-450s with the further purification of gas from carbon dioxide and the synthesis of ammonia at 300 at and methanol at 40-70 at. At the same time, synthetic ammonia is carried out using hydrogen, obtained by diffusion from the converted gas, and the hydrogen remaining after separation, the converted gas is subjected to carbon monoxide conversion, hydrogen is again extracted by the diffusion method, the residual hydrocarbons are converted and then purified from carbon dioxide to a content of 3-7% after blowing the gas mixed with the hydrogen released during the conversion of carbon monoxide and using it for the synthesis of methanol.

The method is carried out as follows.

A gas of 100 thousand tons purified from sulfur compounds is mixed with steam to the steam: gas ratio

4: 1 and the resulting vapor-gas mixture is sent to a catalytic steam reforming reactor; methane at where the conversion is carried out to produce a converted gas of the following composition: CH 2.87; COrj 6.3;

with 8.66; H, 0 17.3; 56. The hydrogen formed during the conversion process is isolated in a diffusion chamber at 500 ° C, structurally integrated with the reactor through a selective hydrogen permeable membrane. Non-diffused converted gas containing 7% СНд-, 16% COj 22%, 11% H 44%, is cooled to a heat exchanger and-. sent to a carbon monoxide conversion reactor. Converted gas formed in the process of CO conversion and containing CH 7.3%, CO 4.73%; СО 32.85%; HQI. 21.71%; 3.2%; NQ of 1.4%, in the amount of 214 thousand nanometers, is fed to a diffusion apparatus, where 27 thousand nanometers of hydrogen are emitted, the required amount of water vapor is added to the undiffered converted gas (about 5-10%) and the conversion is gas in the reactor at. The resulting converted gas containing 1% methane, 16% CO; 25% COij .; 21% to 37%, cooled down in the heat exchanger and subjected to partial conversion of CO in the apparatus to its content of 12%. In this case, the degree of CO conversion is regulated by changing the amount of converted gas transferred through the bypass.

Then the gas is cooled in the heat exchanger up to 40 s and fed to the compartment, in which the partial purification of gas from COri is carried out, the composition of the gas after purification is C02.28%; 21% CH4.J 58% H; 7.4% 1.5% 3.0% y, and its amount is 96.5 thousand nm / h. After that, the hydrogen released in the apparatus is added to the gas, and the resulting synthesis gas is sent to compress to 50 atm. in the compressor and served in the methanol synthesis cycle. Purge gases from the methanol synthesis cycle containing 10% 5% CO; 7% CO and 68% Hg are used for desulfurization.

The 270000 nm hydrogen released through the hydrogen permeable membrane is mixed with the nitrogen required to form the nitric mixture, the resulting nitric mixture is cooled in a heat exchanger until compressed with a compressor to a pressure of 300 atm and sent to the ammonia synthesis cycle. The total ratio of hydrogen going for ammonia synthesis to methanol synthesis gas is 270000 nm: 123500 nm, i.e. the ratio of 2: .1.

The proposed method for producing ammonia and methanol makes it possible to produce 0.34 tons of methanol per ton of ammonia. At the same time, the total consumption of natural gas for both products is 1195 nm with 8850 kcal / nm, or in conventional fuel less waste - 1520 kg. With separate production of methanol and ammonia, which

Claims (1)

Claim A method of producing ammonia and methanol, including the conversion of hydrocarbons with water vapor on a nickel catalyst at a pressure of 40-70 ata and a temperature of 700-900 ° C, the conversion of carbon monoxide at 400-450 ^ C, the purification of gas from carbon dioxide, the synthesis of ammonia and methanol, characterized in that, in order to simplify the method, hydrogen is isolated from the converted gas by the diffusion method and supplied for the synthesis of ammonia, and the converted gas remaining after hydrogen evolution is subjected to carbon monoxide conversion, hydrogen is again released by the diffusion method, etc. conversion of residual hydrocarbons is carried out, and then carbon dioxide is removed from the COg content of 3-7%, followed by gas mixing with hydrogen released during the conversion of carbon monoxide and feeding it to methanol synthesis.