Method of separating liquid and gas

FIELD: separation.

SUBSTANCE: method comprises uniform distribution and supply of gas-liquid mixture to the structurized members with macroscopic and microscopic structures, impregnating the surface of the members with the liquid to be separated, collecting liquid on the surfaces of the structures, and discharging liquid and gas separately. The liquid in gas phase is converted into the liquid phase by reaching the phase thermodynamic equilibrium of the mixture.

EFFECT: enhanced efficiency.

3 cl, 3 dwg

 

The invention relates to the separation technique and can be used in gas, oil and petrochemical industries.

Known method of separating liquid from gas, described in the patent of the Russian Federation No. 2168356, MKI 7, 01 J 19/32, including the uniform distribution and supply of gas-liquid mixtures in structured elements, the wetting of the surface elements of the separated liquid accumulation on the surface structures of the liquid with subsequent separate drainage and gas.

The disadvantage of this method is low efficiency of separation of liquid from gas, because of the separated mixture enters the separation is not in equilibrium due to the lower pressure, and hence temperature at the inlet of the mixture and the nodes separation and plane-parallel motion of the partial phases, which leads to the accumulation of fluid in the outlet line at equilibrium phases.

This disadvantage is partially removed in the method according to the patent of Russian Federation №2186617, MKI 01 J 19/32, 01 D 3/28, which includes the uniform distribution and supply of gas-liquid mixtures in structured elements with the volume of macro - and microstructures, wetting of the surface elements of the separated liquid accumulation on the surface structures of the liquid with subsequent separate drain and the separated gas, the bulk liquid the spine is given unseparated flow in microstructures.

However, the effectiveness of separation of liquid from gas remains low:

- due to the lack of forces to move the particles of the liquid on the surface of structures with plane-parallel motion;

- due to insufficient time for the condensation of liquid in the separation.

Due to insufficient separation efficiency of the fluid drops in the piping downstream of the separator when reaching thermodynamic equilibrium phases, i.e. there are deadweight losses of fluid and challenges in the pipeline network while transporting two-phase mixture.

The present invention is to improve the efficiency of separation of liquid from gas.

The technical result is achieved in that in the method of separating liquid from gas in non-equilibrium state of the mixture at the selected separation parameters, including:

- uniform distribution and supply of gas-liquid mixtures in structured elements with the volume of macro - and microstructures;

- wetting of the surface elements of the separated liquid;

- accumulation on the surface structures of the liquid with subsequent separate drain and separated gas

from the gas phase skip the liquid in the gas phase, in the liquid by bringing the mixture to phase thermodynamic equilibrium, maintaining the required time her PR is the tenure of structured elements, and liquid drop on the surface, the transfer of liquid on the surface of the elements perform rotational spiral movement, at least one phase, the movement phase of the spiral is produced with axial velocity equal to the amount of 1-1,75 radial flow moving phase spiral produce oscillations with respect to wavelength to amplitude equal to

Extract the required residence time of the separated mixture in structured elements leads her into a state of thermodynamic phase equilibrium with the additional condensation of the liquid separated from the gas stream.

Pressure loss in fittings and input nodes of the pre-separation, which is always available, reduce the gas mixture temperature immediately before the separation process, violating phase equilibrium. Achievement of phase equilibria provides a complete transition of the condensed liquid from the gas phase into the liquid phase at the chosen parameters, the separation of the flow (pressure and temperature). This leads to an increase in the volume of the separated fluid, the increase in the diameter of the droplets and their number, which, consequently, increases the efficiency of the separation process liquid from the gas transfer its rotational movement of the mixture on the surface of macro - and microstructures.

Moving at least one of the phases in a spiral axial velocity, equal to the value (1-1,75) radial velocity, leads to increase in time phase in each element and to the initiation and maintenance of the transverse components of the forces, under the action of which the liquid droplets are dropped continuously on the surface of macro - and microstructures. This technique increases the efficiency of separation of liquid from gas. The formation of oscillation phases, while moving them in a spiral, with the ratio of wavelength to amplitude 4-8 leads to additional increase in time phase in each element, additional mixing and, consequently, to improve the efficiency of the separation process liquid from gas in almost constant hydraulic resistance.

The applicant and the authors of the current level of technology is unknown how the separation of liquid from gas, which would apply the above techniques.

Figure 1 shows the three layers of structured elements that are deployed in relation to each other by 90°with the scheme of the movement phase, in which the macrostructure in the form of inclined channels formed by the two pairs of intersecting surfaces, of which one pair is inclined and the microstructure formed by the surface of the porous material; figure 2 presents the cross-section of the structured elements; figure 3 - is viginia spiral flow in adjacent channels; figure 4 - grooved elements and the movement of the spiral flow along it.

In structured items 1 volumes macro 2 and microstructures 3 evenly serves non-equilibrium gas-liquid mixture 4, since the pressure in the pipeline and the inlet fitting is always greater than the pressure in the separator is approximately 0.03-0.05 MPa. The surface elements 5 and 6 are wetted by the liquid. The liquid 7 is accumulated on the surfaces 5 and 6 and is discharged separately from the gas phase 8. For removal of free liquids from the gas only two or three layers of structured elements, for condensation and subsequent separation requires a greater number of layers. Adjacent (adjacent two pairs) surfaces 5 and 6 (figure 2) form a sloping channels - volume macrostructure 2 elements 1, which moves the separated gas stream. At least one of the surfaces 5 or 6 runs of a porous material or sheet material with a porous coating. The porous material or the coating forms a well-developed interfacial contact surface of the microstructure of the 3 elements 1 and the drainage system, which plays the condensed liquid.

In the bottom two or three layers of items 1 to produce the separation of liquid from gas, separated from gas condensate remaining in the gas liquid mixture by bringing it to the phase thermodynami the definition of equilibrium at the actual pressures and temperatures separation by providing the required residence time in them.

The residence time of the separated gas in structured elements provide a path length of its passing, and the rotational spiral movement, at least one of the phases, such as gas, provide within the macrostructure 2, each element 1, the transfer of condensed water droplets on the surface of the elements, for example a gas stream 9 (3), transferred to a drop of liquid on the surface 5 and 6, which simultaneously increases the length of the path of the mixture, therefore, and time phases. Spiral motion phases is provided by the swirler posted before entry into structured elements or executed directly in the channels of the microstructure, for example, the blades 10, which may be made by stamping, i.e. the contour angle of the side surfaces 5 and(or) 6. In the channel macrostructure 2 stream 4 share:

- on thread 11 drawn through the holes 12 of the surface 5 and/or 6)at an angle up in the adjacent channel macrostructure 2;

- the rest of the thread 13, which through oppositely located openings 14 of the surface 5, serves stream 15 at an angle upward.

The selection of the gas stream 11 from the macrostructure in one direction and filing it with the stream offset 15 in the other direction creates a rotational moment, providing a spiral motion, for example, gas stream 9. The selection of the Asti flow of the microstructure 2 and submission in her part of the stream from opposite macrostructure contribute to the alignment of their concentrations due to mixing.

The movement phase of the spiral is produced with axial velocity equal to the amount of 1-1,75 from radial velocity, which depends on the angle of inclination of the blades 10, at an angle of inclination of the blades 45° axial velocity is radial.

When moving phase 7 and(or) 8 spiral (to further increase the efficiency of mass transfer between the gas and liquid flows and increasing the length of the path of movement) make it wobble with respect to wavelength to amplitude 4-8, which is provided by the corrugation of the surfaces 5 and(or) 6 with the corresponding ratio of the step pattern to the height of the ribs (figure 4).

EXAMPLE

Natural gas with liquid under a pressure of 7.6 MPa and a temperature of minus 20°comes from the pipeline through the inlet into the separator where the pressure separation is 7.57 MPa. As at the entrance to the office is changing the parameters of the separation process, the mixture is in a nonequilibrium state. Natural gas in the volume of 210,000 m3/h, with potential content of condensed under these conditions the fluid in the number 1113 kg/h is fed to a separation in two-three layers of structured elements (layer height 150 mm), resulting from it is allocated 1050 kg/h of liquid quantity can be measured in separators or calculated from the amount of volatile liquid product at 1000 m gas, or determined by the potential difference of the liquid content in the gas and the amount of fluid in the pipeline after separation). The separated gas with the content of 63 kg/h neskondensirovannyh liquid:

- serves and evenly distribute in structured elements with the volume of macro - and microstructures;

- condense bringing the mixture in thermodynamic phase equilibrium exposure time;

- spin the mixture gas flows;

- moisten the surface elements condensed drops of the remaining fluid in the amount of 63 kg/h;

- assign the microstructures 42 kg/h

The ablation fluid (loss) drip in the form of gas is 21 kg/h Calculation of the required time to bring the liquid and gas phase thermodynamic equilibrium is conducted according to known dependencies:

M=DFΔSLτ/δkg

(see Angladeshi, Vmem, Czigan. The processes and apparatuses of chemical technology. Goskomizdat, M., 1982, str-574),

where D is the diffusion coefficient;

F - contact surface phases, m2;

ΔSLthe change in concentration over the thickness of the layer, kg/m3;

δ - the thickness of the liquid film, m;

τ - time;

M - number of defenderemos substance from one phase to another, kg;

D - 1,28×10-9m2/s for key com is onenew water methanol, to exclude the ingress of water and aqueous solutions in the pipeline after the separation process;

F - 337,5 m2for a separator with a diameter of 1.8 m on the performance of 210,000 m3/h at a height of Packed layer of one meter with a specific surface area of 135 m2/m3;

δ - 0,0024 m 63 kg liquid and the surface;

ΔSL- 0,6572 kg/m3the average value of the concentration change in the layer thickness of the liquid film;

M - 63 kg, the number defenderemos substance per hour, including key components (water and methanol) 1.23 kg

For the specified values of the residence time of gas in structured elements to achieve thermodynamic equilibrium phases should be τ≥5,3 C. Consequently, the height of structured elements in the working gas velocity of 0.3 m/s should not be less than 1.6 m, taking into account the spiral movement of the gas stream at an angle of inclination of the helix 45° height must be not less than 0.8 m

Thus, the application of the proposed method allows to bring the system liquid-gas in thermodynamic equilibrium directly in the separation process, condensing additional amount of fluid to separate the condensed liquid and to prevent it in the pipeline after system separation.

1. The method of separation of liquid from gas, including uniform is the distribution and supply of gas-liquid mixtures in structured elements with the volume of macro - and microstructures, wetting of the surface elements of the separated liquid accumulation on the surface structures of the liquid with subsequent separate drain and the separated gas, characterized in that from the gas phase skip the liquid in the gas phase, in the liquid by bringing the mixture to phase thermodynamic equilibrium for maintaining the required time of her stay in the structured elements, and liquid drop on the surface.

2. The method according to claim 1, characterized in that the transfer of liquid on the surface of the elements perform rotational spiral movement, at least one of the phases.

3. The method according to claim 1, characterized in that the moving phase of the spiral is produced with axial velocity equal to 1-1,75 radial velocity of the stream.

4. The method according to claim 1 or 2, characterized in that during the movement phase of the spiral make it wobble with respect to wavelength to amplitude equal to 4-8.



 

Same patents:

FIELD: petrochemical industry; oil-refining industry; chemical and other industries; devices for realization mass-exchange processes in the column apparatuses.

SUBSTANCE: the invention is pertaining to the devices for realization of mass-exchange processes in the column apparatuses used both in the systems of a liquid-liquid type and in the systems of a vapor-liquid type and may be used in petrochemical, oil-refining, chemical and other industries. The mass-exchange head includes a row of rectangular platesinclined to each other at an angle with a flanging towards to each other in the upper part of the plates. The rectangular plates of no more than 1 mm thick are made with a perforation in the form of a louver gauze, in which the slit louver holes have a width S equal to 0.3-0.5 mm and with a step equal to no more than the thickness of the plates, with an inclination at an angle α equal to 30-45°, the ratio of the plate length 1 to its width S - from 13 up to 25, a direction of the louver channels to the horizontal axis of coordinates at an angle β equal to 30-45° and with the spacing interval between the louver channels of 1-2 mm. The flangings are facing each other are connected among themselves without a clearance and form a blind bin with the overflow slats in height of no less than the values of a water seal. The inclined rectangular plates with the perforation in the form of a louver gauze in vertexes of the lower angles are connected by the blind plates, which form among themselves a drain branch pipe dipped into the blind bin with the overflow plates of the below lying row of the inclined plates. The advantage of the offered design of the mass-exchange head is expansion of the range of its stable operation at a high efficiency of the mass exchange both in the systems of the liquid -liquid type and in the systems of vapor-liquid type.

EFFECT: the invention ensures expansion of the range of the mass-exchange head stable operation at a high efficiency of the mass exchange both in the systems of the liquid -liquid type and in the systems of vapor-liquid type.

2 cl, 5 dwg

FIELD: chemical industry; petrochemical industry; heat-and-power engineering and other industries.

SUBSTANCE: the invention is pertaining to distributing-contacting devices for the mass-exchange devices and may be used in chemical industry, petrochemical industry, heat-and-power engineering and other branches of industry. The distributing-contacting device contains a distribution plate supplied with a screen with holes, overflow branch-pipes, overflow devices, deflecting shields, perforated truncated cones. The perforated truncated cones are made out of a sheet of no more than 1 mm thick with shutter-type splits of a width -"S" equal to 0.3-0.5 mm, and with a step not exceeding the thickness of the sheet and with an inclination in direction of the liquid motion at an angle α equal to 30-45°, the ratio of the length "1" to its width "S" is from 13 up to 25, a direction of the shutter channels to the horizontal axis of coordinates is at an angle β is equal to 30-45° and the overflow branch-pipes. At that for the packed columns on the ends of the drain branch-pipes at the calculated space intervals there are spray washers, and for plate-type columns the liquid from the drain branch pipes is fed onto an underlying sheet of a plate through a hydraulic lock. The presented distributing-contacting device ensures a high efficiency of the mass-exchange parameters in a wide range of a stable operation of packed columns and in the plate column apparatuses.

EFFECT: the invention ensures a high efficiency of the mass-exchange parameters in a wide range of a stable operation of the packed columns and the plate column apparatuses.

3 cl, 3 dwg

FIELD: chemical industry; fine gas separation from a liquid at reconstruction of separators and filter-separators of the absorbing and rectifying columns.

SUBSTANCE: the invention is dealt with the field of chemical industry and intended for fine separation of gas from a liquid at reconstruction of separators and filter-separators of the absorptive and rectifying columns. The multi-cartridge ring-type separating nozzle contains: a cover, a filtering unit, a device of water separation, an inlet connection pipe connected with the filtering unit by a pin, gas-distributing discs fixed to the pin. The filtering unit is made in the form of mesh cartridges mounted one on another. At that the internal surfaces of the mesh cartridges form a gas-distributing collector. The device of water separation is made in the form of the overflowing pipes located in the cartridges and mounted under them the drain pans with the axial apertures. Each mesh cartridge is supplied with a baffle made in the form of a plain disk with an axial aperture and a ring-type bead along the disc perimeter. Each mesh is formed by simultaneous winding of two parallel bands of the mesh, one of which is made out of a flat mesh, and the other - out of a corrugated mesh. On the side of its cylindrical internal surface a mesh cartridge is supplied with a cylindrical perforated shell. At that the first layers of the mesh band are fixed to the perforated shell by metal staples or welded to the perforated shell. At least two external layers of each mesh band are fixed by metal staples. The number of the mesh cartridges makes 6. The overflowing pipes are installed uniformly around the nozzle on a circumference, diameter of which makes from 0.85 up to 0.92 of the external diameter of the mesh cartridge and the diameter of a flow area of each overflowing pipe makes from 0.038 up to 0.05 of the external diameter of a mesh cartridge, and the total area of apertures of the shell perforation makes from 50 up to 60 % of the area of the internal cylindrical surface of the shell. In result the invention allows to increase efficiency of separation at the expense of prevention of the separated liquid accumulation in the cartridges of the nozzle.

EFFECT: the invention ensures increase efficiency of separation and prevention of the separated liquid accumulation in the cartridges of the nozzle.

2 cl, 1 dwg

Regular nozzle // 2232632
The invention relates to structures designed to conduct heat and mass transfer processes in a variety of technological devices in the system, gas (vapor) - liquid, and can find application in chemical and other industries

The invention relates to contact devices for mass-transfer apparatus, in particular for Packed columns for gas - liquid

The invention relates to constructions of regular nozzles for heat and mass transfer apparatus

The invention relates to mass transfer devices column apparatus for liquid - liquid and can be used in petrochemical, chemical and other industries

The invention relates to mass transfer equipment used in absorption and distillation columns

The invention relates to constructions of regular nozzles designed to conduct heat and mass transfer processes in the gas(vapor) - liquid, and can find application in gas, petrochemical and other related industries

Film apparatus // 2260466

FIELD: apparatus for performing heat- and mass-exchange processes in gas-liquid systems; chemical, food-processing and microbiological industries.

SUBSTANCE: proposed apparatus has housing, horizontal partitions, contact tubes fitted with distributing branch pipes and helical spirals. Mounted in between horizontal partitions forming the gas inlet chamber coaxially with contact tubes and distributing branch pipes secured on lower horizontal partition are gas-and-liquid distributors consisting of plates located radially relative to distributing branch pipes forming slots for flow of gas. Upper end faces of plates are provided with blank secured on horizontal partition; lower ends of plates are lowered into circular clearance formed by inner surface of contact tube and outer surface of distributing branch pipe; at least two plates located near each other are provided with inserts at side end faces which form passage for liquid together with plates; this passage is communicated with chamber for introducing the liquid through holes made in blank. Side surfaces of distributing branch pipes have holes for flow of liquid. Plates of gas-and-liquid distributor are mounted tangentially relative to side surface of distributing branch pipe.

EFFECT: smooth distribution of liquid over perimeter of contact tubes; increased area of passage of liquid into circular clearance; avoidance of deposits on surfaces of distributing branch pipes.

3 cl, 5 dwg

FIELD: physical or chemical processes and apparatus.

SUBSTANCE: device is made of cylindrical housing with horizontal axis and rotatable shaft with nozzle having developed surface that is made say of disks. The bottom section of the housing is provided with receiving and overflow recesses provided with branch pipes for supplying and discharging liquid. The top section of the housing is provided with branch pipes for supplying and discharging vapor. The horizontal size of the recesses and branch pipes for supplying and discharging vapor is equal to the length of the housing generatrix.

EFFECT: enhanced reliability and efficiency.

3 dwg

FIELD: chemical engineering.

SUBSTANCE: apparatus comprises groups of parallel rectangular plates with corrugated bottom. The ribs of the corrugation are oriented along the flow, and the distance between the plates does not exceed 30 mm. Between the plates, rods or pipes are arranged at an angle 90±15° to the vector of flows. The plates are assembled in groups of parallel plates inclined downstream. The uniform distribution of fluid over the plates when fluid flows from one plate group to another group is provided by means of distributing-overflowing devices.

EFFECT: decreased hydraulic drag.

2 cl, 5 dwg

The invention relates to designs of heat and mass transfer devices and can be used in chemical, food and pharmaceutical industries

The invention relates to contact devices for mass-transfer apparatus, in particular for Packed columns for gas - liquid

The invention relates to a device for holding heat and mass transfer processes such as distillation, adsorption, condensation of steam, cooling the gas-vapor mixtures, gas purification, etc., and can be used in chemical, petrochemical, oil refining, metallurgical, pulp and paper and other industries

The invention relates to processes of contact fluid for subsequent separation by absorption and rectification between gas and liquid at the extraction or separation of the emulsion, separation and coalescence fine liquid droplets in the gas stream and may find application in gas, petrochemical, oil, food and other industries

The invention relates to equipment of heat and mass transfer processes, such as distillation, absorption, condensation of the steam, cooling the gas-vapor mixtures and others, and can be used in chemical, petroleum refining and related industries

The invention relates to catalytic means for catalytic treatment of exhaust gas

FIELD: chemical engineering.

SUBSTANCE: apparatus comprises groups of parallel rectangular plates with corrugated bottom. The ribs of the corrugation are oriented along the flow, and the distance between the plates does not exceed 30 mm. Between the plates, rods or pipes are arranged at an angle 90±15° to the vector of flows. The plates are assembled in groups of parallel plates inclined downstream. The uniform distribution of fluid over the plates when fluid flows from one plate group to another group is provided by means of distributing-overflowing devices.

EFFECT: decreased hydraulic drag.

2 cl, 5 dwg

Up!