The method of supplying natural gas to energy technology installation of ammonia production

 

The invention relates to the field of industrial power engineering and chemical technology and can be used to obtain the synthesis gas in the production of synthetic ammonia. In the method of supplying natural gas to the power and process plant for production of ammonia by compression to a pressure of 4.1-4.5 MPa, hemosorption-catalytic desulfurization of compressed natural gas at a temperature of 350-400With, dispensing steam medium pressure 3,8-4,2 MPa in natural gas, steam and air-steam catalytic conversion in a tubular furnace and shaft reactor at a pressure of 2.9 to 3.8 MPa and a temperature of 500-1010With compressed air driven by a condensing steam turbine, two-stage conversion of carbon monoxide, gas purification from carbon dioxide thin doocastle gas method mahanirvana, booster compression of the produced synthesis gas to drive steam turbines operating at high-pressure steam from 9.6 to 10.6 MPa and having a selection of steam medium pressure generating superheated vapour high pressure (from 9.6 to 10.6 MPa) by using the heat of the technological processes, the heat of the flue gases in the furnace and in the auxiliary boiler, siati the Ara high pressure of 9.6 to 10.6 MPa, with subsequent dosage of the missing quantity of steam medium pressure in the resulting gas-vapor mixture, and hemosorption-the catalytic desulfurization of natural gas is performed at a pressure of 2.0-4.0 MPa to compress it in the jet compressor. The invention allows to reduce energy consumption, reduce capital expenditures and repairs, as well as to improve the reliability of the equipment. 1 Il.

The invention relates to the field of industrial power engineering and chemical technology and can be used to obtain the synthesis gas in the production of synthetic ammonia.

Large-tonnage production of synthetic ammonia requires large quantities of energy and material resources, therefore, the most important is the development of technological schemes of production based on the energy technology combine to enhance the efficiency of its production.

There is a method of natural gas in energy technology installation by throttling device for lowering the pressure 11 and lowering the pressure on getprotocol turbine 7, produces electrical energy (see SU 1231237 A1, class F 01 K 13/00, 15.05.1986).

The disadvantage of this method is of limited use.

A known method of supplying p is underwater gas compressor driven by a condensing steam turbine operating on a pair of medium pressure hemosorption-the catalytic desulfurization of compressed natural gas, a steam catalytic conversion in a tubular furnace and shaft reactor, the compression process air, two-stage conversion of carbon monoxide, the cleaning gas from carbon dioxide, a thin gas purification method mahanirvana, booster compression produced synthesis gas (Handbook of apothica. - M.: Chemistry, 1986, S. 110-118, Fig.11-31).

The known method has the disadvantage that the natural gas before feeding it to hemosorption-catalytic desulfurization is compressed in a two-stage compressor. This decreases the reliability of the equipment desulfurization and accordingly the entire energy technology installation.

Known methods closest to the proposed invention is a method of supplying natural gas to the power and process plant for production of ammonia by compression to a pressure of 4.1-4.5 MPa, hemosorption-catalytic desulfurization of compressed natural gas at a temperature of 350-400With, dispensing steam medium pressure 3,8-4,2 MPa in natural gas, steam and air-steam catalytic conversion in a tubular furnace and shaft reactor at a pressure of 2.9 to 3.8 is rbine, two-stage conversion of carbon monoxide, gas purification from carbon dioxide thin gas purification method mahanirvana, booster compression of the produced synthesis gas to drive steam turbines operating at high-pressure steam from 9.6 to 10.6 MPa and having a selection of steam medium pressure generating superheated vapour high pressure (from 9.6 to 10.6 MPa) by using the heat of the technological processes, the heat of the flue gases in the furnace and in the auxiliary boiler (see Process regulation reconstruction ammonia production JSC “Nevinnomyssky Nitrogen, installation of the technological scheme No. 1B-2271-TX-3, 1B-2279-TX-3, 1B-2321-TX-3).

The disadvantage of this method is wasteful expenditure of energy on the throttling of natural gas coming from backbone networks to a pressure of 1.7 to 3.0 MPa, because natural gas is then again compressed in the compressor to 4.1-4.5 MPa. In addition, the use of expensive and sophisticated equipment, which is a compressor driven by a condensing steam turbine, leads to an increase in capital expenditures, increases the cost of the repair and maintenance of equipment and reduces the reliability of the production.

The technical result, to achieve the spending, repairs and improving the reliability of,

This technical result is achieved in that in the method of supplying natural gas to the power and process plant for production of ammonia by compression to a pressure of 4.1-4.5 MPa, hemosorption-catalytic desulfurization of compressed natural gas at a temperature of 350-400With dispensing steam medium pressure 3,8-4,2 MPa in natural gas, steam and air-steam catalytic conversion in a tubular furnace and shaft reactor at a pressure of 2.9 to 3.8 MPa and a temperature of 500-1010With compressed air driven by a condensing steam turbine, two-stage conversion of carbon monoxide, gas purification from carbon dioxide thin gas purification method mahanirvana, booster compression of the produced synthesis gas to drive steam turbines operating at high-pressure steam from 9.6 to 10.6 MPa and having a selection of steam medium pressure generating superheated vapour high pressure (from 9.6 to 10.6 MPa) by using the heat of the technological processes, the heat of the flue gases in the furnace and in the auxiliary boiler, compression of natural gas from the pressure of 2,0-4,0 MPa to a pressure of 4.1-4.5 MPa is carried out in jet COA steam medium pressure in the resulting gas-vapor mixture, and hemosorption-the catalytic desulfurization of natural gas is performed at a pressure of 2.0-4.0 MPa to compress it in the jet compressor.

The drawing shows a schematic diagram for implementing the method.

The method includes the following stages: hemosorption-catalytic desulfurization 1, the compression of natural gas in the jet compressor 2, the dosing of the missing pair medium pressure 3, steam and air-steam catalytic conversion in a tubular furnace 4 and the shaft reactor 5, which includes the generation of superheated vapour high pressure of 9.7 to 10.6 MPa) by using the heat of the technological processes, the heat of the flue gases in the furnace and in the auxiliary boiler 6 and boiler-utilizers 7, air compression 8, two-step conversion of carbon monoxide 9, the cleaning gas from the carbon dioxide 10, a thin gas purification method mahanirvana 11, booster compression produced synthesis gas 12 driven by a steam turbine 13, working at high-pressure steam. Installation for implementing the method also includes condensing steam turbine 14 to drive the air compressor. Steam turbine 13 has a selection of steam medium pressure 15. Steam drives 16 provide other compny compressor serves on line 18. Steam medium pressure is metered into a gas-vapor mixture after jet compressor through line 19. Compressed and purified synthesis gas in line 20 is supplied to the ammonia synthesis. The condensate line 21 is displayed on the side. Steam medium-pressure line 22 is fed to the turbines other compressors, exhausters, pumps and other auxiliary purposes.

The method of supplying natural gas to the power and process plant for production of ammonia is carried out as follows.

Natural gas line 17 is supplied from backbone networks under a pressure of 2.0-4.0 MPa and purified from sulfur compounds in the plant hemosorption-catalytic desulfurization 1. Then the purified natural gas is fed into the jet compressor 2, where it is compressed to a pressure of 4.1-4.5 MPa due to the energy of compression of high-pressure steam of 9.7 to 10.6 MPa coming from the steam line 18. Received after the jet compressor, the gas-vapor mixture in line 19 dispense the necessary amount of steam medium pressure to the desired ratio of the vapor - gas conversion processes. Go through all production stages 4, 5, 9, 10, 11 and 12, the compressed and purified synthesis gas in line 20 is supplied to the synthesis answersa for compression of natural gas in the jet compressor 2, the remaining quantity of high-pressure steam is supplied to the turbine booster compressor syngas 13, having a selection of steam medium-pressure line 15. After the turbine booster compressor syngas 13 steam condenses and together with other condensate line 21 is displayed on the side.

Steam medium pressure obtained in the selection of the turbine 13, spent a process for the conversion of natural gas through line 19, the turbine air compressor, turbines other compressors, exhausters, pumps, and other auxiliary purposes in line 22.

Example 1.

In accordance with the invention presents a method for production of synthesis gas for ammonia production with a capacity of 1,360 tons/day of natural gas from backbone networks with a pressure of 4.0 MPa. In the jet compressor natural gas in the number 28600 kg/hour is compressed to a pressure of 4.2 MPa due to the energy of high-pressure steam 10.0 MPa. For these parameters the estimated coefficient of the injection jet compressor is 1.9. The flow rate of steam at high pressure jet compressor - 15 t/h. The total number produced by high-pressure steam - 325 t/h, are spent:

- 15 t/h on jet compressor;

the C-gas 270 t/h of steam medium pressure 4.0 MPa, are spent:

- 100 t/h for injection into natural gas for carrying out the process of conversion;

- 65 t/h on the turbine air compressor;

- 75 t/h on other turbine compressors, exhausters and pumps;

- 30 t/h for auxiliary purposes.

As couples after tripping in the jet compressor remains in the natural gas, replacing a portion of the metered steam medium pressure, the intensity of his work in the jet compressor is equivalent to the intensity of the high-pressure steam, creativesage in the turbine operating with a pressure of 4.0 MPa and equal to 43.5 kW/so the energy intensity of the steam medium pressure creativesage in condensing turbines equal to 193 kW/so

The energy consumption for compression of natural gas are:

N=1543.5=652,5 kW.

For comparison, the energy consumption for compression of natural gas:

in similar -3500 kW;

in the prototype -1250 kW.

Example 2.

Presents a method for production of synthesis gas for ammonia production with the main operating parameters, as in example 1, but under the pressure of natural gas coming from backbone networks with a pressure of 2.0 MPa. In the jet compressor natural gas in clickedrow work the estimated coefficient of the injection jet compressor is 0,38. The flow rate of steam at high pressure jet compressor - 75 t/h. The total number produced by high-pressure steam - 340 t/h, are spent:

- 75 t/h jet compressor;

- 265 t/h on the turbine booster compressor syngas.

In the selection of the turbine booster compressor syngas -210 t/h of steam medium pressure 4.0 MPa, are spent:

- 40 t/h for injection into natural gas for carrying out the process of conversion;

- 65 t/h on the turbine air compressor;

- 75 t/h on other turbine compressors, exhausters and pumps;

- 30 t/h for auxiliary purposes.

The energy consumption for compression of natural gas are:

N=7543,5=3262,5 kW.

This is slightly lower than in similar, but higher than in the prototype. Calculations determined that the lower limit of the pressure of the natural gas coming from the backbone network, wherein the method is effective, is the pressure of 2.0 MPa. This efficiency is determined by the above energy costs for compression of natural gas, as well as the capital cost savings, increased reliability and reduced volume and cost of repairs.

The formula of the way it is compressed to a pressure of 4.1-4.5 MPa, hemosorption-catalytic desulfurization of compressed natural gas at a temperature of 350-400With, dispensing steam medium pressure 3,8-4,2 MPa in natural gas, steam and air-steam catalytic conversion in a tubular furnace and shaft reactor at a pressure of 2.9 to 3.8 MPa and a temperature of 500-1010With compressed air driven by a condensing steam turbine, two-stage conversion of carbon monoxide, gas purification from carbon dioxide thin gas purification method mahanirvana, booster compression of the produced synthesis gas to drive steam turbines operating at high-pressure steam from 9.6 to 10.6 MPa and having a selection of steam medium pressure generating superheated vapour high pressure (from 9.6 to 10.6 MPa) by using the heat of the technological processes, the heat of the flue gases in the furnace and in the auxiliary boiler, characterized in that the compression of natural gas from the pressure of 2,0-4,0 MPa to a pressure of 4.1-4.5 MPa is carried out in the jet compressor using high-pressure steam from 9.6 to 10.6 MPa, with subsequent dosage of the missing quantity of steam medium pressure in the resulting gas-vapor mixture, and hemosorption-catalytic desulfurization nature of the Sabbath.

 

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