SU939895A1 - Installation for producing liquid and gaseous carbon dioxide - Google Patents

Description

Coil gas from the gas mixture is eipad1 COij. Condensated gases by reverse flow through a recuperative heat exchanger are released into the atmosphere. After filling one of the freezers with dry ice, the flow of the gas mixture is switched to another freezer, and the first is supplied with a SOch gas with a pressure of qtmie 5.11 bar from the tank with liquid COgi. The COH vapor is condensed, and the dry ice is liquefied, and liquid COii is drained into the tank. To obtain dry ice from liquid CO, press.

A disadvantage of the known installation is that there is no equipment for deep drying of the gas mixture entering the installation, which should lead to clogging of the heat exchanger with water ice, low-temperature pipelines, fittings and freezers COij, i.e. to reduce the working period of the installation, and, consequently, to reduce its performance.

In addition, the disadvantage of the known installation lies in the fact that the long time of defrosting of the frozen CO and its overflow into the collecting tank leads to the downtime of the installation, which also reduces its performance.

The purpose of the invention is to increase plant productivity by preventing moisture from entering the freezer and shortening the freeze-thaw time of carbon dioxide.

This goal is achieved by the fact that a plant for producing liquid and gaseous carbon dioxide, including a flue gas compressor installed in series, a recuperative heat exchanger, a carbon dioxide freezer with a chiller, a collection tank of liquid carbon dioxide, is equipped with an additional heat exchanger to freeze moisture. . a call connected at the inlet with the lower part of the collecting tank and a flue gas compressor, and at the exit with the upper part of the collecting tank and with the entrance of the recuperative heat exchanger ...

In addition, the installation is equipped with a gas blower connected at the inlet with the upper part of the collecting tank and the release of carbon dioxide gas from the additional heat exchanger, and at the outlet with the carbon dioxide freezer.

The scheme of the proposed installation is shown in the drawing.

The installation consists of a compressor 1, additional heat exchangers 2 for lush moisture removal, from flue gases and evaporation of liquid dioxide

carbon, heat exchanger 3, refrigerant 4 carbon dioxide freezers, machine 5, storage tank b, liquid carbon dioxide separator 7 and gas blower 8.

The installation works as follows.

The carbon dioxide-containing gas mixture, such as dihal gases, is compressed.

the compressor 1 is cooled in its end refrigerator with dropping of moisture and is supplied to alternately connected heat exchangers 2, where further cooling of the flue gases and almost complete freezing of moisture from them takes place. In the heat sealer 3, the flue gases are cooled to a temperature close to the saturation temperature by reverse flow.

exhaust flue gases, and go into one of the carbon dioxide 4 freezers, working alternately, in the 4 COrj freezer, carbon dioxide in the form of dry ice on the cooled surface falls out of the flue gases. Cooling of the freezers is carried out by the chilling machine 5. After filling one of the freezers CO ,. dry ice flue flow and

D, the refrigerant flow 5 of the refrigerating machine 5 is switched to another freezer 4, where the formation of dry ice also begins. To turn frozen on the surface of the mold 4. dry ice in the liquid state is supplied with heat by supplying gaseous COij at a pressure higher than at the triple point. With this gas, C0 0 (i is condensed, and liquid COti from the freezer 4 C0 (i is discharged into tank 6). To accelerate the overflow on the supply line of the gaseous COfj, from the additional heat exchanger 2 to

A blower 8 is installed after the separator 7 of liquid carbon dioxide after the separator 7 of the liquid carbon dioxide 8. Liquid CO is periodically taken from the container b, and partially COij gas in the form of finished products.

Claims (2)

Primer p. Before entering the compressor into the compressor; 1, the flue gases, as in any other method of obtaining CO (j), water is preliminarily cooled from a temperature of 250–350 ° C to a temperature of 30–30 ° C, followed by separation of the condensed moisture. After compression in compressor 1 The flue gases are again cooled in a water heat exchanger. As a result of cooling water with water, the main, but not the full amount of moisture from the sparse gases is emitted. In the installation scheme this is a well-known equipment not shown. These chambers, which work alternately, cool the flue gases and freeze the moisture due to the cold evaporation of liquid COij, derived from collection 6. Per 1 kg of product and with the following parameters Installation work: initial COti concentration in flue gases is 15-20% by volume, flue gas pressure ISlO na, flue gas temperature at the outlet of additional heat exchangers from -20 to -35 ° C, flue gas temperature to additional heat Enzo 20Z C, the temperature of the liquid COi in the tank 6 from -40 to -45 ° C and a pressure of 10-10 Pa-- to freeze moisture and cool the flue gases consumes the necessary amount of heat q 65-80 kcal / kg CO, in which heat exchangers 2, 0.8-1.0 kg of liquid COrj is supplied. The gases liberated from moisture are cooled in the recuperative heat exchanger 3 and fed to the freezers 4, where carbon dioxide in a solid phase is precipitated on a cooled refrigerating machine 5 from them. If the freezer is sufficiently filled, the solid freezer SOD (1 kg in the example) freezer ayut from holo spinning machine and the flue gas collector and making it into the thawing of frozen COq by feeding into it a gaseous COtj. from heat exchangers 2. Gaseous CO, heating solid CO, is condensed, giving away the latent heat of vaporization in the amount of 80 kcal / kg CO 2 (at system pressure). The amount of heat required for liquefying solid COrj is equal to the heat of fusion — 65 kcal / kg CO2. An excess amount of heat corresponds to an excess amount of gaseous COrj in an amount of up to 0.2 kg, which is taken as a finished product for the needs of the consumer. The plant's supply is supplemented with a heat exchanger, which provides for the deep drying of flue gases at the expense of internal resources, and a gas blower, which accelerates the thawing of carbon-dioxide freezers, which leads to an increase in the plant's productivity, since this increases the operating time and period and reduces the defrosting time of carbon dioxide freeze-up. Claim 1. An apparatus for producing liquid and gaseous carbon dioxide, preferably from flue gases, comprising a flue gas compressor installed in series; recuperative heat exchanger, carbon dioxide freezer with chilling machine and liquid carbon dioxide collecting tank, so that in order to improve performance by preventing moisture from entering into the freezer and shortening the time of defrosting of carbon dioxide, the plant is equipped with an additional a heat exchanger for freezing moisture from the flue gases connected at the inlet to the lower part of the collecting tank and the flue gas compressor, and at the outlet c. the upper part of the collecting tank and the inlet of the recuperative heat exchanger. 2. Installation according to claim 1, characterized in that it is equipped with a gas blower connected at the inlet with the upper part of the collecting vessel and with the release of gaseous carbon dioxide from the additional heat exchanger and at the outlet with the freezer of carbon dioxide. Sources of information taken into account in the examination 1. The author's certificate of the USSR 393397, cl. F 25 G 29/00, 1971. 2. US Patent 2,738,658, cl. 62-12, 1956 (prototype). GZHG. STR .-m