Method of recuperation of heat

FIELD: updated methods of recuperation of heat in CO2 discharge systems in production of ethylene oxide.

SUBSTANCE: proposed method includes absorption of ethylene oxide from circulating gas flow by washing the gas in scrubber. Washed flow of circulating gas is brought in contact with hot absorbing carbonate solution for absorption of CO2 and flow of circulating gas after absorption of CO2 returning it to ethylene oxide production cycle; proposed method includes also bringing the said washed circulating gas flow in contact with heated liquid after removal of ethylene oxide at first contact stage, transferring the preheated circulating gas to stage of absorption by hot carbonate for removal of CO2, cooling the said circulating gas from stage of absorption by carbonate and removal of carbonate from it by bringing it in contact with said liquid from first contact stage at second contact stage after cooling this liquid, transferring the liquid from second contact stage to first contact stage and transferring the cooled circulating gas from second contact stage to reaction system for obtaining the ethylene oxide.

EFFECT: enhanced operational and economical efficiency of heat recuperation.

1 dwg, 1 ex

 

Background of invention

The scope to which the invention relates.

The present invention relates to an improved method of heat recovery in the system of removal of carbon dioxide in the process of producing ethylene oxide.

Description of current level of technology

In some manufacturing processes, such as upon receipt of ethylene oxide by oxidation of ethylene with molecular oxygen, the oxidation process is also generated carbon dioxide. The carbon dioxide so produced must be removed to prevent the accumulation of this product in the system. Cm. U.S. patent No. 3523957.

The removal of carbon dioxide from the reaction system to obtain ethylene oxide is carried out, as a rule, in hot carbonate system, washing with potassium carbonate), where the reaction gas after the removal of the target product of ethylene oxide by washing with water in the scrubber fully or partially served in the absorber CO2. The washed gas from the reaction system after the removal of ethylene oxide, as a rule, is cold and has a temperature of scrubber or, in the case of repeated compression after washing, some of the above-mentioned temperature. In addition, this circulating gas is saturated with water in these cold areas. If this gas is sent directly the NGOs in the absorber CO 2then it cools wash solution of carbonate. When the heat supplied to the circulating gas due to the heat of solution of carbonate, and also due to evaporation of water up to saturation of the gas at the higher operating temperature of the absorber CO2there is a loss of heat contained in the carbonate solution. This heat, or energy, must be filled in udobochnoy section (regenerator) removal system CO2where the carbonate solution is heated by steam to ensure that emissions of carbon dioxide into the atmosphere.

In addition to heating the gas entering the absorber, it is also necessary to cool the gas after its exit from the absorber to remove water before the gas is returned to the reaction system to obtain ethylene oxide, since water is harmful to the catalyst reaction system. In addition, to prevent catalyst receipt of ethylene oxide from possible contamination by carbonate, it is necessary to wash out the gas after exiting the absorber water to prevent entrainment of carbonate in the reaction section. Usually referred to gas cooling and washing are performed in two separate operations. Cooling is performed in a conventional heat exchanger, and rinsing in wash column. Upon cooling, gas heat lost to cooling water.

Increasing economic characteristics of the heat recovery is in such processes is desirable since even a slight increase in efficiency leads to significant savings in connection with krupnomasshtabnogo installations world-class production of ethylene oxide.

Brief description of the invention

In accordance with the present invention the flow of circulating gas from the reaction system to obtain ethylene oxide after removal of ethylene oxide prior to the absorption of CO2heated by direct contact with circulating water flow, which, in turn, is heated by direct contact with the flow of recirculating gas returned after absorption of CO2in the reaction system of ethylene oxide. Thus, the circulating gas is cooled in the process of extraction of ethylene oxide by washing, heated and saturated with water at an elevated temperature before feeding it into the absorption system hot carbonate. Unwanted cooling and heat loss of the carbonate system are minimized. After removal of the CO2circulating gas before returning to the reaction system is cooled and cleaned of residual carbonate and reduce water content by contact with the cooled circulating water flow that is used for heating the circulating gas. The heat contained in the gas returned from the absorber CO effectively transmitted recirculating gas supplied to the absorption of CO2.

Brief description of drawing

On the accompanying drawing shows schematically the implementation of the invention.

Detailed description of the invention

Drawing does not show the usual scheme of production of ethylene oxide by oxidation of ethylene with molecular oxygen and conventional extraction system of ethylene oxide with water. These operations are well known and widely used in industrial practice.

The drawing shows a pre-saturator 1, containing the upper section 6 and a lower section 5, and each section provides a close contact of steam with the liquid. Preferably, each section is equipped with an inert nozzle to facilitate contact of steam with the liquid.

Circulating the gas from the reactor oxidation of ethylene after absorption of the ethylene oxide in the scrubber through line 4 into the bottom section 5 pre-saturator 1. The circulating gas is introduced through line 4, after washing in the scrubber, is relatively cold, for example, has a temperature of from 32 to 50°C. In the lower section 5 of this circulating gas is in close contact with the heated water flow from the upper section 6, which comes in section 5 via line 7. The water stream is introduced through line 7, has a temperature of, for example, from 70 to 85°C.

As a result of contact in which eccii 5 the flow of circulating gas is heated to a temperature of from about 65 to 80° C and saturated with water at this temperature. This circulating heated gas is fed via line 8 at a known stage of absorption of the hot carbonate where gas is removed FROM2formed during oxidation of ethylene. Because the circulating gas is heated in a pre-saturator before entering the absorber hot carbonate, cooling the hot carbonate flux is minimized.

The water stream after contact flows through line 9 from the bottom of section 5 pre-saturator 1 in refrigerator 10, where further cooling of the stream, for example, to a temperature of from 40 to 45°C. Chilled water stream flows through line 11 into the upper section 6 pre-saturator 1, where the chilled water flow coming into close contact with the circulating gas is returned through line 12 from the stage of absorption of the hot carbonate, and cools it.

In section 6 of the circulating gas is simultaneously cooled and washed from the contained carbonate, which otherwise adversely affects the catalyst obtain ethylene oxide, if he was returned to the reactor obtain ethylene oxide.

Of section 6 of the water stream after contact, now heated, for example, up to 65-85°C, flows through line 7 to the lower section 5, where, as described above, pre-heats cirkuliruyusiy gas before entering the absorption of a hot carbonate.

The cooled circulating gas having a temperature of, for example, from 45 to 48°, which contains negligible amounts of carbonate and reduced the amount of water compared with the stream in line 12, through line 13 in the form of recycling to the reaction system to obtain ethylene oxide.

The application of the present invention in the form shown in the drawing, provides a number of significant advantages over known systems. In addition to heat recovery circulating gas leaving absorber CO2you can apply very high costs of wash water, allowing more efficient leaching compared with the known isolated wash system. In addition, the pressure drop of the circulating gas is smaller than in the case of using a heat exchanger. This contributes to the reduction of energy consumption in the reaction system for ethylene oxide.

Another advantage that is very important for the system to absorb hot carbonate is the reduction of residual ethylene oxide in the circulating gas entering the absorber CO2. Generally, the absorption of the ethylene oxide from the circulating gas a small amount of ethylene oxide remains in the gas. When gas washing system hot carbonate this residual ethylene oxide is reversed in glycol, which accumulates in the process stream to remove it through the valve of release of CO2. This glycol pollute the environment, and often have to take measures to remove it. Reduction of residual ethylene oxide in the gas stream entering the absorber is particularly important to maintain low level of CO2in the reaction system for ethylene oxide, since the number of circulating gas into the absorber increases. For example, when the concentration of CO2in the gas after the oxidation of ethylene to 7% (vol.) in the absorber serves only approximately 20% of total circulating gas. However, if you want to maintain the concentration of CO21% (vol.), in the above-mentioned absorber serves the whole of the circulating gas, which can cause an increase in the number of the resulting glycol 5 times, if not to reduce the amount of residual ethylene oxide in the gas stream entering the absorber.

The following example illustrates the invention with reference to the accompanying drawing.

Example

In a plant for the production of ethylene oxide with a capacity of 600,000 t/yr flow 4 circulating gas from the reaction system after absorption of the ethylene oxide in the version of the technology with a low content of CO2has a massive speed 13300 kg·mol/h; the CO2extending t is in the typical case of 2.2% (vol.) and the water content of 0.39% (vol.). The residual content of ethylene oxide is 30 million-1(vol.). The temperature of the gas 41°and the pressure of 20.0 bar (2 MPa). Speed circulating flow of water is approximately 7 70400 kg·mol/h, and its temperature 43°C. This recirculating flow of water after exiting hatakeda section 6 is heated to 79.3°C. This water is introduced into contact with the circulating gas is supplied by a nozzle section 5 pre-saturator 1. The gas is heated to 77°and the liquid is cooled to 57°C. From a liquid to a gas is passed approximately 28,2 million kcal (118.0 m kJ). The temperature of the gas rises to 77°and the water content is increased to 2.12% (vol.). The content of ethylene oxide in the gas entering the absorber CO2reduced by 60%.

Water from gazoochistnoe section 5 pumped by the pump and is cooled in heat exchanger 10 to 43°, then return to the upper part hatakeda section 6. At the top of the quench this water is introduced into contact with the gas flowing from the absorber CO2in section 6, also provided with a nozzle. The gas returned from the absorber CO2on line 12, has a temperature of 98°and the water content of 3.6% (vol.). This gas section 6 is cooled by circulating water up to 45°C, while the water content is reduced to 0,49% (vol.). In addition to cooling, circulares the th gas captures ethylene oxide, dissolved in water in the lower section 5, the content of ethylene oxide increases from zero in the stream 12 that is returned from the absorber to 17.5 million-1(vol.) in the stream 13. Thus, removing 60% of the ethylene oxide contained in the source gas.

The circulating gas is returned to the reaction system through line 13, is the CO2decreased in the absorber from 2.1% (vol.) in the source gas to 1.0% (vol.). The pressure of the return gas is 19.7 bar (1.97 MPa), suggesting that the differential pressure across the system is only 0.3 bar (30 kPa), of which 0.2 bar (20 kPa) falls on the pre-saturator 1. When using conventional heat exchanger pressure drop is approximately 0.6 bar (60 kPa).

In this example, achieved the following objectives in accordance with the present invention. Approximately 62% of the heat contained in the gas stream 12 from the absorber CO2, Recuperat and transmit the circulating gas flowing to the absorber CO2. The gas is returned to the absorber CO2washed and cooled, reaching a reduction of its moisture content. The residual content of ethylene oxide in the gas fed to the absorber CO2reduce by 60%. These goals have been achieved at a lower pressure drop in comparison with the known solution.

The scale of the installation mi is a new class for the production of ethylene oxide is significant savings.

For professionals it is obvious that the sections 5 and 6, shown in the drawing as an integral part of the same pre-saturator may represent separate units or can be combined with other devices, for example with the absorber CO2. The essence of the process remains unchanged, and sections 5 and 6 operate in the same manner as described above.

The method of producing ethylene oxide, in which the ethylene oxide is absorbed from the flow of circulating gas by washing in the Laundry, washed the flow of circulating gas is introduced into contact with hot absorptive carbonate solution for absorption of CO2and the flow of circulating gas after the absorption of CO2return to the cycle of the production of ethylene oxide, characterized in that it includes an introduction to the contact mentioned rinsed flow of circulating gas after removal of the ethylene oxide in the first contact stage with a heated aqueous fluid to preheat washed mentioned flow of the circulating gas and the absorption therein of ethylene oxide and mentioned cooling water liquid transfer mentioned circulating heated gas phase absorption hot carbonate for the removal of CO2the mentioned cooling the circulating gas from the stage absorption carbonate and removing from it the way carbonate is put into contact in the second contact stage with the said aqueous liquid with the first contact stage after cooling mentioned aqueous liquid, the transfer of liquid water from the second contact stage in the first contact stage and transfer the cooled circulating gas with said second contact stage in the reaction system of ethylene oxide.



 

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