PORTABLE MODULAR APPARATUS FOR RETAINING, DIAGNOSING AND MEASURING OF PROPPANT AND FORMATION SOLIDS IN HYDROCARBON PRODUCING WELLS

Abstract

The present disclosure relates to equipment, procedures, and materials for the diagnosis and control of formation and/or fracture granular solids from hydrocarbon-producing zones, produced during the operation of wells in the oil industry. This surface technology does not require the use of repair equipment and relies on filtering elements and sieves installed in a high-efficiency equipment that takes advantage of the cyclonic effect of phase separation, designed, and built to safeguard the integrity of the equipment and surface conduction lines.

Description

CROSS-REFERENCE TO RELATED APPLICATIONS

This patent application claims priority under 35 U.S.C. Section 119 to Mexican Patent Application No. MX/a/2023/002359, filed Feb. 24, 2023, the entire disclosure of which is incorporated herein by reference.

FIELD

The present disclosure relates to equipment, procedures and materials for both the diagnosis and control of formation and/or proppant solids coming from underground drilling, produced during the operation of hydrocarbon wells; and is a surface technology that makes use of filtering elements and screens in a high efficiency equipment, specially designed to protect the integrity of the equipment and surface pipelines. The present disclosure also relates to analysis, installation and removal procedures of such solids without the use of repair equipment. The present disclosure further relates to repair and maintenance operations of wells in hydrocarbon reservoirs.

BACKGROUND

Solids production during hydrocarbon exploitation is a main issue in unconsolidated formations and/or producing fields subject to induced hydraulic fracking with proppant materials. This is explained by the fact that forces due to fluid drag phenomena on the fractured walls and grain shapes exceed the cohesive strength of the cementitious material. Since these forces depend on the kinetic energy of the fluid, on the friction between the fluid and the porous medium and also on the size of the surface in contact (Bergendhal, 2008), the larger the exposed surface, the greater the forces generated, which is why the production of these solids gradually increases until it critically affects the productivity of the wells. Additionally, the presence of gases can induce corrosion damage to pumps, valves, pipes and other equipment, plus the risk of inducing well uncontrol (Ortiz, V. M, 2016). Other problems related to solids production include induced changes of properties of working fluids and the increase in associated costs, instability of the well walls, erosion and/or collapse of pipes, erosion of downhole and surface equipment and others no less critical such as the accumulation of solids at both, the well bottom and surface, also formation collapse and loss of the well (Cirilo, 2016). Therefore, the control of solids production, that is, the removal of as much solids as possible with specially designed equipment, is a fundamental task during production operations. Several technologies are available in the market for monitoring and control of solids production (Table 1), which seek not only to know the volume of solids production, but also to separate them from other fluids. The most important ones are described below.

Technologies for Phase Separation

Venturi type separators. In these separators, a gas-solid particles mix is passed through the nozzle of a Venturi tube; a liquid is injected into the Venturi and when it meets the solids, it generates small droplets, which retain the solids transported by the gas to produce the separation of gas and solids (FIG. 3). However, oftentimes It is necessary to cool the hot gases whose temperature is higher than the boiling temperature of water, in addition, the gas is saturated with the steam that is produced (Duroudier, J. P., 2016). The same reference indicates that their use is most effective when the gas velocity is greater than the velocity of the water droplets with embedded particles. Some disadvantages of these systems include: i) the potential formation of highly corrosive acidic solutions; ii) the high efficiency of this equipment is associated with high pressure drops and therefore high energy consumption with the corresponding associated costs, iii) the solid byproducts go through drying processes and their disposal can incur in high associated costs, iv) it is necessary to postprocess the water used during this process and, v) water recovery and solids drying of the produced sludge makes the potential reuse of solids more expensive (Pandit, 2015).

Separation vats. These systems include a vessel of composite geometry, typically a cylindrical upper section and a conical lower section, arranged in a vertical position, with one inlet and two outlets. Duroudier (op. cit.) points out that this equipment is designed to separate liquid vesicles present in a gas phase, when the liquid bodies are solutions of solids such as in crystallization processes. The inlet of the mixture is tangential to the cylindrical section where the solids are dragged by the gas and it rises to be separated, in addition, since the inlet is tangential, separation also occurs by the centrifugal trajectory. An important condition for the success of this technology is that the gas velocity must be similar to the free fall velocity of the solids. These separators are usually larger than both, gas separators and horizontal separators.

Disc decanter. This equipment, illustrated in FIG. 4, acts on dispersions and allows the separation of solids and liquids of different densities by means of centrifugal action. The dispersion is fed at the top center and distributed through the bottom to a series of disc plates; in these, the liquids migrate upwards and the solids towards the walls of the vessel containing them. This device requires frequent cleaning and maintenance of the vessel where the solids are stored (Duroudier, J. P., 2016).

Tubular decanter. It consists of a vertical cylinder into which a dispersion is poured. The clarified liquids exit at the end opposite to the inlet of the dispersion and the solids from the discharge accumulate at the bottom of the cylinder on its side wall. Once the flow to the cylinder is interrupted, the accumulated solids must be removed; for this reason, the operation of this equipment must be programmed to make interruptions for maintenance; this also means that the production line must include these programmed stops.

Screw based sludge separator. A horizontal version of this equipment, shown in FIG. 5, designed to clarify fluids and separate them from solids in a dispersion, is reported optimized for increased inlet flow rate and particle size. This separator includes a horizontal cylinder that rotates at a controllable speed between 1,200 and 3,000 rpm and reaches diameters of up to 2 m. Duroudier (2016) points out that the volume of sludge in the dispersion should not be greater than 40% of the total volume to operate efficiently. In its axial region, the separator has a wide wing screw that also rotates at a slightly different speed than the cylinder. This screw conveys the sludge to the area opposite the dispersion inlet. A conical termination at the sludge outlet end forces the sludge out near the longitudinal axis and causes the sludge to densify and emerge; the liquids exit the equipment through a diaphragm for final filtration. Duroudier (Op. Cit.), proposes that the solids throughput be evaluated with the expression:

$Q_B=N_{VR}p\pi \left(r_B^2-r_I^2\right)$

where:

• • N_VR: is rotational speed of the screw with respect to the vessel (rev/s),
  • P: screw pitch,
  • r_B: internal radius of the vessel,
  • r_I: radius of the interface separating the thickened sludge from the liquid.

From the previous expression one can see that to increase the solids separation rate it is necessary to increase the rotation speed of the screw, which requires high energy consumption and a larger internal radius of the vessel to increase the rate of solids separated with this system.

Other separators designed to separate hot gas-liquid mixtures include vessels in which this thermal condition is exploited to separate the gas phase from the liquid phase by driving the latter upward in a vertical column or channeling it through outlet valves; these separators include gas separators, separator vats, vertical and horizontal flash drums, and degassers. Typical examples of such equipment are vertical gas separators and horizontal separators which, as examples, are described below.

• • a) Vertical separators. These consist of vertical cylinders with spherical ends; in them the gas-liquid mixture is injected at half height of the cylinder, in this way the gas is discharged upwards, and the liquid, by the action of gravity, downwards where it accumulates. To improve this separation and prior to the gas outlet, a mesh is placed to capture and condense microdroplets and precipitate them to the bottom of the cylinder (Duroudier, 2016). Evidently these systems are exclusively oriented to gas-liquid mixtures; additionally, and since the difference in density of crude oil and water aided by gravity allows them to be used as gas, oil and water separators, they are also considered as three-phase separators, however, when there is production of sands, clays, foamy components or other high-viscosity components, the efficiency of these separators is drastically reduced; Also, the residence time of the crude oil is required to be longer, so the dimensions of these separators must increase significantly along with their cost.
  • b) Horizontal separators (degassers) are horizontal cylinders whose free surface of the liquid is 4 to 8 times larger than that of the previous water separators; these equipments also have screens to capture, condense and collect microdroplets at the bottom of the vessel, this facilitates the degassing process (Duroudier, 2016). These equipments must satisfy a minimum residence time, a specific flowrate, the mixture feed pipe must be kept flooded to create a hydraulic protection and the liquid direction must not be tangential to the ferrule; although designed to increase their separation area and volume, they are not particularly efficient when the mixture in the fluid matrix includes solids and reservoir water in large volumes that must be separated from the gas. A design that addresses this problem in the case of a sudden increase in water volume or when large gas bubbles are produced is the use of double horizontal cylinders, one upper horizontal and one lower horizontal, however, this configuration is appropriate when there is little or no solids production.
  • c) Spherical separators are separators whose main storage has the shape of a sphere, they also have the advantage of their compact size and proper gas handling; they are smaller than cylindrical separators and are especially efficient in the separation of two-phase fluids, typically gas and liquids, in limited areas such as platforms; however, when there is production of sands, clays, foamy components or unexpected increases in the flow, they drastically reduce their efficiency.

Cyclone separator applications in industry. Cyclone-based technologies have been used since the last century with great developments until today, with successes associated to their standardization and control of both, energy and volumetric efficiencies; their applications include the on-line measurement of volumetric flow in multiphase fluids using cyclone separators for phase separation and then the measurement of each phase separately with Coriolis-type flow meters for the separated gas and liquid phases (Godoy-Alcántar et al., 2008); other applications include emission control, product recovery, combustion improving, heating, spray film drying, material and liquid sampling and monitoring, fluid filtration, industrial and domestic vacuum cleaners (Funk & Baker, 2013), also include heat exchangers, gasification and combustion of solid fuels, coal pyrolysis, solid waste separation in fluidized beds (Nakhaei et al., 2019) and foam breaking (Hoffmann, & Stein, 2007) and post-pneumatic particulate transport.

Richardson, J. F. et al., (2002) summarizes in general terms the applications of this equipment in industry:

• • (a) Separation of particles (suspended in a liquid of lower density) by size or density, or more generally, by fall velocity.
  • (b) the removal of suspended solids from a liquid.
  • (c) separation of immiscible liquids of different densities.
  • (d) dehydration of suspensions to obtain a more concentrated product.
  • (e) the breaking of liquid-liquid or gas-liquid dispersions.
  • (f) removal of gases dissolved in liquids.

Solids control methods include those listed in Table 1.

Description of conventional cyclone separators. For a correct interpretation of this section, the table at the end of this section shows a list of abbreviations and acronyms.

Cyclone separators have been extensively studied and developed since the beginning of the last century; in their initial standard configuration, they include four elements; a leading line and inlet to the main body called the inlet tube (denoted at (a) in FIG. 6), a main body (denoted at (b) in FIG. 6), a conical section (denoted at (c) in FIG. 6) with an outlet end, and an outlet section at its top end, called the vortex locator (denoted at (d) in FIG. 6). This cyclone separator configuration was developed by Shepherd & Lapple in the 1930s-1940s (Cited by Funk et al., 2013, and Mahender et al., 2016), and is also illustrated in FIG. 9, it includes the aforementioned sections, which are described below:

TABLE 1
Methods of solids control in hydrocarbons producing wells.
Method        Description
Design        Selective and oriented drilling
              Optimization of hydraulic
              fracturing design.
              Drilling design optimization.
Mechanical    Use of flexible tubing
              Rigid or expandable strainers
              Slotted liners
              Settling tank
              Desanders
              Deslimers
              Sludge cleaners
              Decanting centrifuge
              Cyclones.
Geomechanical Gravel packers
and Chemical  Chemical stabilization
Alternatives  Simple dilution
              Dilution with displacement
              Inhibition by encapsulation
              (PHPA or PAC).

• • a) The inlet tube of the multiphase fluid (denoted at (a) in FIG. 6) is lodged tangentially with respect to the main body, as illustrated in FIG. 7; its longitudinal axis may form a right angle or be inclined with respect to the vertical (FIG. 1). In their cross section, they are designed in circular or rectangular section, as schematized in FIG. 8. Another characteristic is that the inlet nozzle to the main body can be straight or conical in section, as illustrated in FIG. 2. In cases of highly erosive fluids, the inner wall is treated to reduce the effect of erosion.
  • b) Main body or “barrel”. The longitudinal axis of this element (denoted at (b) in FIG. 6) can be vertical and in some cases horizontal (Dodbiba, & Fujita, 2004); its diameter is typically several times larger than that corresponding to the inlet pipe. The reviewed literature indicates that studies have been done on its optimum diameter and length, and the relative position of the inlet pipe in it, this position is mainly due to the following aspects: first, to the residence time required for fluid separation in the case of GLCC (see glossary at the end of this chapter); then, to minimize the entrainment of liquid micro droplets towards the gas outlet and finally to avoid the formation of liquid films on the inner wall of the element (denoted at (d) in FIG. 6) and in the case of GSCC to reduce the amount of smaller solids travelling towards the outlet element (6d).
  • c) Conical section (denoted at (c) in FIG. 6). The fundamental principle of these separators is the use of rotational and gravity effects on multiphase fluids to separate solids of different diameters and/or liquids of different densities. Particularly, in those separators with a conical end, the radius of the rotational path is gradually reduced with the fall, allowing small diameter particles to be separated from those of larger diameter that precipitate to the bottom of the separator, while the smaller ones travel towards the vortex locator element, at a higher outlet.
  • d) Vortex locator. This element located at the top of the separator is typically a hollow cylindrical element whose longitudinal axis is collinear with the axis of the main body (denoted at (d) in FIG. 6), it allows, depending on the phases to be separated, to receive and channel i) the smallest solid particles in case of GSCC, ii) gases in case of GSCC, iii) gases in case of GLCC and iv) liquids of lower density in case of LLCC.

The flowrate, velocity and geometric properties of the above model have been extensively studied to either increase collection efficiency or reduce pressure drops; Funk et al., (2013) shows different designs of more representative cyclone dust separators on the timeline, reproduced here in FIG. 9.

Classical kinetics of particle motion in cyclones. The side inlet connection (FIG. 10) drives the fluid particles, arriving at the main body, to enter tangentially, then the fluid molecules are subjected to a rotational field affected by gravity; the heavier fluid molecules are forced radially to the wall of the larger diameter cylinder and, at the same time, downward in the direction of the gravitational forces.

The angular velocity at the access nozzle can be evaluated knowing the separator geometry and the inlet velocity, as shown in FIG. 11, where, for a separator of radius R with inlet nozzle inclined an angle α₀, through which a particle circulates at velocity V_T, and assuming R₂ as the critical radius, the angular velocity ω is evaluated as:

$\omega =\frac{V_T}{R_2/\cos {\alpha }_0}$

From the above equation, keeping the inclination angle α₀ constant, if ω increases, the tangential velocity increases.

From the above equation, the centripetal force Fc can be calculated as (Funk, Op. Cit.):

$F_C=\frac{m{V}_T^2}{R_2}=m{\omega }^2{R}_2$

Where:

• • m: mass of the particle,
  • R: radius of the cylindrical section of the separator,
  • R₂: major radius of the particle trajectory, assumed elliptical at least in the middle of its trajectory,
  • α₀ is the angle of inclination of the separator inlet tube,
  • V=V_T: inlet velocity of the particle assumed as inlet tangential velocity,
  • ω: inlet angular velocity of the particle,
  • FC: centrifugal force of the particle.

A relevant conclusion from the above equation is that when R₂ decreases, the Fc force increases, this is exploited in conical geometry changes that cause an upward vortex and selective transport of lighter molecules and/or particles upwards, while heavier molecules and/or solid particles are trapped in a downward gravitational field.

Other arrival tube geometries. New developments in cyclone separators include variations in geometry and angle of the inlet tube, as shown in FIGS. 1 and 2, where:

(a) Documentary information found indicates that horizontal angles, perpendicular to the main body axis (denoted at (a) in FIG. 1) facilitates stratification of fluids of different LLCC densities at low velocity and with sufficient residence times in the inlet tube.

b) For inlet angles forming between 25° and 30° with the horizontal, the separation of fluids of different densities of the GLCC type is before the outlet, so processes can be optimized by installing other inlet ducts to the main body to channel gaseous fluids in a pre-separation stage (Barahona, B. T. R., 2016). Kuba Et al., (1995) has determined that angles of 27° allow stratification for the conditions indicated.

FIG. 1 shows the schematic of the angle of incidence between the inlet tube and the main body in cyclone separators, where the angle of arrival, α:

(a) Horizontal inlet tube: It facilitates the formation of stratified flows between liquids of different densities at low flow velocities, α=0 (Barahona, B. T. R. R., 2016; Kouba et al, 1995).

b) Inlet tubes at angles α between 25° and 30° with the horizontal (denoted at (b) in FIG. 1), facilitate the separation of fluids of different densities of the gas-liquid (GL) type before the outlet, so that processes can be optimized by installing other conduits to the main body to channel gaseous fluids in a pre-separation stage (Barahona, Op. Cit.); coincidentally, Kuba et al, (1995) has determined that angles of 27° allow stratification for the conditions indicated in their technical document.

c) Steeply inclined inlet tubes (denoted at (c) in FIG. 1). Tubes with these angles induce agitated flow patterns, more influenced by gravity, typically used for liquid-gas phase separation. Reported inclination angles are in the range 60°<<<66°.

FIG. 2 shows the diagrams of the different conditions of the pipes arriving to the Main body of the separator, that is:

(d) Conical inlet tube (denoted at (d) in FIG. 2): it induces the acceleration of the mixture at the outlet to reach separation velocities; with the increase of the velocity, it is sought to increase the separation efficiency.

e) Double inlet (denoted at (e) in FIG. 2): Accelerates the separation of the gas phase and the liquid phase in steady state; under these conditions it can be programmed to maintain flow conditions and a pre-phase separation stage where stratification is promoted; more suitable for medium to low residence times.

f) Rectangular inlet (denoted at (f) in FIG. 2): by decreasing the rectangular cross section at the arrival to the main body, as shown in the circles with dotted line, it is sought to increase the volume at arrival, and at the same time, increase the flow velocity; rectangular inlet denoted at (f) in FIG. 2 shows: i) isometric view and ii) elevation view.

g) Circular inlet with helical inner wall (denoted at (g) in FIG. 2). This type of wall has been proposed to apply a rotation to the particles/molecules around one of its axes and in favor of their fall. The aim is to accelerate the separation process by making the pressure drops at the outlet of the inlet tube, inside the main body, less relevant.

Recent Studies on Cyclone Separators

Change in the main body. New studies on the geometry of cyclone separators and fluid kinematics have led to the modification of geometries where the conical section has been replaced by an extension of the cylindrical section and, at its bottom, a vortex limiter, LV, as shown in FIG. 12, modifying the geometry of the main body and the vortex locator; In cases where the density difference between the media to be separated is significant, these geometries allow reducing the frictional energy losses along the path of the solids inside the separator and at the same time increasing its efficiency by increasing its length (Gutiérrez-Torres et al., 2005); by placing a vortex delimiter at the bottom of the vessel, this prevents the vortex from coming into contact with the materials deposited on the bottom by dragging them upwards and reducing their separation capacity (Hoffmann & Stein, 2007). A wide variety of gas-solid-liquid separator designs and geometries exist with these designs, including those that include (FIG. 14): conical vortex finder geometries (FIG. 14A) that seek to accelerate the flow velocity at the inlet and capture larger volumes of gases, they also seek vortex control and efficiency by raising or lowering the vortex boundary plate; Other designs include blade systems within the main body (FIG. 14B) to accelerate higher density molecules and/or particles towards the walls of the main body and get them out through a side outlet at its bottom and, at the same time, control the direction of the vortex carrying lighter molecules; for the separation of vapors and liquids, others include propellers to graduate the separation speed and stimulate the formation of inverse vortices (FIG. 14C); Other designs include (FIG. 14D) the use of a plurality of cyclones within a single vessel, taking advantage of the principle that the centrifugal force on a molecule or particle on the inner wall of the separator is inversely proportional to the radius of the gas outlet pipe, one or more plates with tubing are responsible for isolating the clean gas zone and that of the other components of higher density.

Vortex locator (VL). The design of cyclone separators requires optimizing each of their elements, such is the case of vortex locators where their shape, dimensions, relative position with respect to the main body, and recently their configuration has been studied; W. Xu, et al. (2016), introduce and report new features aiming to optimize the performance of these devices (FIG. 13); they argue that the experimental models and their corresponding CFD models of straight cylindrical VL's affect the flow pattern reducing their efficiency, for this reason, researchers propose to modify the conventional cylindrical geometry of vortex locators with a truncated inverted cone-shaped and slotted louvered blade separator (SVF); according to the authors, these modifications induce additional gas flow into the walls of the conical element and into its slots. Xu notes that this modification increased the efficiency of a separator.

Reported advantages of cyclone separators include (Hoffman & Stein, 2008; González, G. J. C., 2015; Richardson, Op. Cit.):

• • Competitive investment costs with respect to other equivalent separation technologies.
  • Control of gas and oil separation capacity.
  • Ability to operate at high temperatures.
  • Ability to operate at high pressures.
  • Can be designed to receive chemically aggressive fluid matrices.
  • Low installation and maintenance costs.
  • Small space requirements for installation and operation, suitable for marine installations.
  • Simple construction with no moving parts in their basic designs.
  • Robust equipment.
  • It can be constructed of different materials depending on its use.
  • It can be designed to accept erosion and/or corrosion resistant coatings or to “repel” particles.
  • Can be constructed from metal plates or cast iron molds.
  • Can handle sticky or adhesive particles with proper irrigation.
  • Can separate solid or liquid particles with proper design.

Some disadvantages include (Hoffman & Stein, 2008; Richardson, J. F. et al., 2002):

• • Depends on the energy with which the flow enters the inlet of the cyclone separator, its design has been oriented to either, increase its separation efficiency, to reach the lowest pressure drop in transit or to control their separation capacity; design efforts have been directed mainly to the first two approaches.
  • Due to the wide variety of cyclone separator designs and variables involved, there are no analytical models that satisfactorily represent them.
  • High abrasive effects of granular solids on the separator walls.
  • Regarding separators with conical termination, it is necessary to have a balanced cone; here, a gaseous flow enters through the apex in the opposite direction to that of the separated solids-liquids to form the counter-flow effect and direct the fluid of lower density towards the vortex locator (ASME, 2011).
  • Other conditions restrict the solids separation and exit process in conical hydrocyclones (ASME, 2011; Richardson, Op. Cit.), among them: inadequate inlet pipe pressure, high viscosity fluid matrix, high solids concentration, high overhead above the cone balance point, excessive outlet moisture and lump formation, excessive vacuum formation, very small apexes, excessive wear localized areas of the cone, combinations of these.
  • Low efficiency for particles with diameters below a critical value.
  • Large pressure drops compared to other systems.

Various patent documents in the art are identified below:

• • Spanish Patent No. 2 264 688 (2007) discloses that the access of the gas/granular product (GS) in this element is preferably tangentially and in its upper part, in addition it requires, in a first stage, a separator with a separator wheel at the height of the inlet and whose details are not specified. Its geometry is cylindrical-conical and requires at least two centrally arranged and rotationally symmetrical built-in elements within the housing of this system. The space between the embedded elements and the casing is important to control separation. It also requires secondary gas sources (potentially air) at its bottom, to generate the upward momentum of fine particles and gas to achieve dual selectivity. This invention claims to achieve not only separation of bulk materials from the gas, but also from the accompanying fine particles. Finally, the fine particles and gas exit through the upper end of the housing and the already separated bulk product exits through its lower end. Since the separation control is also achieved with the gas flow from the bottom of the housing, additional energy is required in addition to the GS source, so its operating costs are significantly increased, in addition, this equipment is designed to separate only gases and solids.

U.S. Pat. No. 10,337,267 B1 (2019) describes a main body tank, an inlet pipe through which the mixture is led into the main body, which may be tangentially connected to it, a vertex finder centered inside the main body; in the upper region a gas outlet pipe whose axis is perpendicular to the symmetry axis of the main body and in its lower region a liquid collector plate. This device is specifically designed to separate gases from liquids and has no possibility to handle granular solids.

U.S. Pat. No. 10,412,820 B2 (2019) describes a separation tank for gas-liquid-solids mixture including a vertical cylindrical structure, as the main body, a lower inlet pipe through which the mixture is led into the main body, which may be tangentially connected thereto, a vortex locator centered inside the main body; in the upper region a gas outlet pipe whose axis is perpendicular to the axis of symmetry of the main body; the natural gases can be processed to obtain hydrogen and carbon to use the hydrogen to produce plasma to melt and vitrify solids making them inert materials. This apparatus is specifically designed to separate liquids and consume the gases by transforming the properties of granular solids.

U.S. Pat. No. 10,533,138 B2 (2020) describes a separation tank for mixing carbonaceous materials in the presence of homogeneous catalysts and liquid organic compounds; in this apparatus the mixture is cooled, depressurized and separated into a gas phase, an oil phase and a water phase. The separation stage is carried out in a vertical cylindrical structure, as the main body, a lower inlet pipe through which the mixture is led to the main body may be tangentially connected to it; inside the main body there are a series of stages, from bottom to top, an attenuating baffle plate, a stage for breaking foams and oscillations, a coalescence stage and a filtering stage; in the upper region there are gas, water and oil outlets. This apparatus is specifically designed to separate the fluids indicated and does not accept any type of solids.

U.S. Pat. No. 10,596,580 B2 (2020) describes a separation tank for solid-liquid mixtures, which includes a vertical structure whose shape is cylindrical-conical in its main body, an inlet pipe through which the mixture is conducted towards the main body, which is tangentially connected to it, a first emulsification stage by means of cyclonic action and a subsequent stage within the same apparatus where the recovery of the remaining liquids in the wet solids takes place by means of an endless screw installed in a pipe whose axial axis is coaxial to the main body, induction of shear forces by means of a vortex process of variable geometry; coalescence and flocculation are induced for extraction of colloidal structures from the fluid and formation of flocs and lumps, also, separation of lumped solids from liquids are carried out by means of a vortex process. This apparatus and processes are not designed to separate solids from gases.

U.S. Pat. No. 10,655,300 B2 (2020) describes a water jet excavation system and includes a hydrocyclone for water recycling purposes; the separation is carried out, in a first stage, in a separation tank; in a second stage, equipment for separating solids from water by means of cylindrical-conical hydrocyclones; the waste material from this stage is conveyed to another drainage system. The description of the system indicates that they are a plurality of conventional cyclones arranged in parallel along one or more axes. The feed is through their upper cylindrical section and the waste solids are channeled through the apex of their conical section into the lower region of the separator; these units are not designed to handle gases other than pressurized air.

U.S. Pat. No. 11,007,542 B2 (2020) describes a separation tank for solids-liquid mixtures that includes a vertical structure whose shape is cylindrical-conical in its main body, an inlet pipe through which the mixture is conducted to the main body, which may be tangentially connected thereto; a vertex finder centered within the main body that includes ribs to induce a vortex in the flow and a plurality of openings therein, and its axis is coaxial to the axis of symmetry of the main body; In the upper region the vortex locator allows the channeling of low density molecules out of the main body, a plurality of openings are also included in the vortex locator that allows the channeling of the fluid from the inlet pipe towards the interior space of the main body. The vortices induced by the ribs channel the higher density molecules or particles towards the lower conical region of the main body. Note that in this case, the vortex locator is directly subject to the flow of the fluid matrix, so it is directly subject to the effect of erosion, which is aggravated by having a multiplicity of openings, and does not exist a prior element of exposure to erosion before reaching the vortex locator, as in the In the case of the slotted tube of the technology described in this document, inducing not only damage to this element, but its direct erosion due to the presence of openings in it. It is not specified, in U.S. Pat. No. 11,007,542 B2, whether the apertures in the vortex finder have been optimized in size, distribution, location and direction with respect to its surface.

In view of the foregoing, the applicant notes that there is a wide range of industrial separator designs for fluid matrices composed of various phases, for example, low, medium and high density fluids and solid particles; their design and operation can be simple or include multiple control systems, as well as be monitored and controlled remotely, however, and as far as the inventors is concerned, none of the investigated separators allows for the removal of flowback solid particles from a fluid matrix at high pressures and high costs in an efficient manner, as is the case of the efficient control of production solids in hydrocarbon wells, therefore, the above technologies are surpassed by the present disclosure, since none of the cited references comprehensively relate to specially developed equipment and methods for solids control that do not require the use of workover equipment, which affect well productivity and the integrity of production systems, pipelines and surface equipment.

SUMMARY

The modular design described in the present disclosure allows that each module, also called Solids separation module, includes filtering elements in its head that cause the separation of solids from the fluid matrix to be highly effective; a final filtering stage facilitates the removal of remaining moisture in the captured solids and allows the evaluation of its production volume for diagnosis. Additionally, its modular architecture allows to quickly expand its separation capacity by connecting two or more modules to meet local requirements during production, increasing the throughput or restricting the particle size to be separated by installing them in parallel or in series, thus reducing downtime and operating costs. Finally, the solids separation modules, by not having parts subject to movement during operation, have the following advantages simultaneously:

• • A) Maintenance is significantly reduced by including built-in elements that are not movable during operation.
  • B) Maintenance costs are reduced by not incorporating movable elements such as bearings, propellers, blades and other similar elements as indicated in Hoffman & Stein, (2007) and in FIG. 14.
  • C) Since the solids separation modules of this disclosure take advantage of the fluids energy coming from the well, no additional energy sources are required for their operation.
  • D) In isolated areas, the incorporation of transportable energy sources such as electric power plants is not required.
  • E) Maintenance times are reduced due to the incorporation of non-movable parts during operation.
  • F) Continuous operation time is extended since this disclosure includes non-moving incorporated parts.

Therefore, one object of the present disclosure is to provide a system for the efficient handling of both, formation solids and proppant produced in wells, hereinafter also called solids, that includes:

• • (a) A procedure for the analysis, installation, and removal of said solids and proppant without the use of conventional workover equipment.
  • b) A solids separation module that, inside its main body, incorporates an element of cylindrical geometry with a pattern of specially directed perforations through which it performs the retention and filtering of formation solids and/or proppant coming from oil or gas wells.
  • c) A system for monitoring formation solids and/or fractures from hydrocarbon wells using the same solids separation module.
  • d) The measurement of the volume of formation solids and/or proppant from fractures, coming from hydrocarbon wells, using a solids collection and monitoring system.
  • e) A system that allows the continuous operation of retention and filtration of formation solids and/or proppant from fractures, without deferring the production of hydrocarbons in their liquid and/or gaseous state, by means of a solids recovery subsystem in an operationally safe manner.

Another object of the present disclosure is to provide a solids separation module that permits to control and separate solids embedded in a two-phase fluid matrix, flowing at pressures up to 2,000.0 psi and temperatures up to 150.0° C.

A further object of the present disclosure is to provide a system of interconnectable solids separation modules which, if connected in a parallel pattern, permit to increase or decrease the flowrate of the two-phase fluid matrix in a controlled manner.

A further object is to provide a system of interconnectable solids separation modules which, if connected in a series pattern, allow to control the gradation of solids coming from a two-phase fluid matrix by increasing or decreasing the number of solids separation modules connected in the system.

Another object of the present disclosure is to provide a solids separation module that takes advantage of the natural energy coming from the wellbore, without requiring any additional energy source to separate the solids from the two-phase fluid matrix.

Another object of the present disclosure is to provide a solids separation module and the manner it is handled, which has applications in different industries, but in particular in the petroleum industry.

For a more complete understanding of the nature and objects of the present disclosure including apparatus, procedures and materials for the diagnosis and control of solids from hydrocarbon producing zones, produced during the operation of wells in the petroleum industry, will be described at length in the subsequent “detailed description” section, and the scope of which will be listed in the appended claims.

Various aspects of the present disclosure are also addressed by the following Paragraphs 1-106 and in the noted combinations thereof, as follows:

Paragraph 1. A system for efficient separation of granular solid materials embedded in a fluid liquid matrix from hydrocarbon wells under conditions of high pressure up to 2,000.00 psi and temperatures up to 150° C., comprising: (a) a subsystem for receiving a fluid liquid matrix mixed with solids; (b) a subsystem for the controlled separation of solids embedded in a fluid liquid matrix by means of a solids separation module; (c) a subsystem comprising both the solids outlet conduit and the fluid matrix outlet conduit; (d) a solids capture and monitoring (FIC) subsystem for analysis of the granular solids and measurement and diagnosis of their production in the target well.

Paragraph 2. The system according to Paragraph 1, wherein it is applicable to wells where the fluid matrix pressure is the pressure of hydrocarbons flowing from wells, in corrosive environments and at operating temperatures of up to 150° C.

Paragraph 3. The system. according to Paragraph 1, wherein the minimum size of the separated granular solids is 35 microns.

Paragraph 4. The system according to Paragraph 1, wherein the maximum size of the separated granular solids is 1200 microns.

Paragraph 5. The system in accordance with Paragraph 1, wherein the receiving of the fluid liquid matrix with solids embedded therein is carried out with piping and surface connections capable of withstanding up to 5,000.00 psi and flowrates of up to ten barrels per minute.

Paragraph 6. The system according to Paragraph 1, wherein the separation of the fluid liquid matrix and the solids embedded therein is carried out with one or a plurality of solids separation modules, each of which includes a main body and a plurality of embodiments.

Paragraph 7. The system according to Paragraphs 1-6, wherein the solids separation module subsystem comprises a main body (CP) and a set of embodiments.

Paragraph 8. The system according to Paragraphs 1 and 7, wherein the solids separation module subsystem comprises a main body comprising: a) cylindrical section (SC); b) inlet tube (TE); c) fixing ring (AF); d) top cap-plug (TC_S); and e) bottom cap-plug (TC_I).

Paragraph 9. The system according to Paragraphs 1 and 7, wherein the solids separation module subsystem comprises the following embodiments: f) slotted tube (TUR); g) wear sleeves (CD); h) cylinder-cover (TAC); i) outlet pipe (TSA); j) strainer (CED); and k) impact plate (PIM).

Paragraph 10. The system according to Paragraphs 7 and 8, wherein the main body of the solids separation module subsystem comprises a vessel made of materials having a minimum yield strength of 36,000.0 psi, wherein the materials comprise carbon steel or other materials.

Paragraph 11. The system according to Paragraphs 7 and 8, wherein the main body of the solids separation module subsystem has cylindrical, spherical, conical, conical, polyhedral or combination thereof geometry, wherein one optional combination comprises a hollow cylindrical-spherical with a longitudinal symmetry axis and a cylindrical section (SC) of straight axis, two hemispherical sections (TC_S and TC_I), one at each of its ends, and is positioned vertically with respect to its longitudinal symmetry axis.

Paragraph 12. The system according to Paragraphs 8 and 11, wherein the cylindrical section of the main body is hollow and has a length to outside diameter ratio (L_SC/DE_SC) of between 1.80 and 3.20, preferably between 1.85 and 2.91; an inside diameter to outside diameter ratio (DI_SC/DE_SC) between 0.81 and 0.99; an inside diameter (DI_SC) preferably between 7.10 inches and 14.50 inches.

Paragraph 13. The system according to Paragraphs 8 and 11, wherein the cylindrical section is made of materials whose yield strength is at least 36,000.00 psi, preferably carbon steel whose thickness is in the range of 0.25 to 0.75 inches.

Paragraph 14. The system according to Paragraphs 8 and 11, wherein the cylindrical section includes in its upper part, a flanged connection that hermetically connects the cylindrical section with the upper cap-plug.

Paragraph 15. The system according to Paragraph 8, wherein the inlet tube (TE) is longitudinally hollow and conveys the fluid matrix containing the solids towards the main body (CP), preferably tangentially connected, wherein its longitudinal axis forms a right or inclined angle with respect to the longitudinal axis of the main body, preferably forming a right angle, wherein its cross-section is of straight or conical section, preferably kept straight until rigidly and hermetically joined to the cylindrical section of the main body.

Paragraph 16. The system according to Paragraph 8, wherein the main body is longitudinally hollow and made of materials whose yield strength is at least 36,000.00 psi, preferably carbon steel.

Paragraph 17. The system according to Paragraph 8, wherein the inlet tube is preferably of straight circular cross-section with a wall thickness in the range of 0.21 inches to 0.42 inches and whose ratio of its inner diameter (DI_TE) to the outer diameter of the main body cylindrical section (DE_SC), DI_TE/DE_SC is preferably in the range of 0.12 to 0.22, and more preferably in the range of 0.15 to 0.19.

Paragraph 18. The system according to Paragraph 8, wherein the fixing ring (AF) is in the form of a ring having an inner diameter, an outer diameter and a thickness, and is fixed to the main body (CP) without any possibility of displacement, concentric to it, in its cylindrical section, wherein its outer diameter fits tightly within the cylindrical section and is nominally equal to the inner diameter of the cylindrical section of the main body and coaxial to it, functioning as a simultaneous support for the grooved tube, the wear sleeves and the wear tube.

Paragraph 19. The system according to Paragraph 18, wherein the fixing ring is made of a material having a minimum yield strength of 36,000.0 psi, preferably carbon steel; wherein said fastening ring is located at a height (H_AF) of 1.94 times its outer diameter, from the lower end of the cylindrical Section, that is H_AF/DE_AF=1.94.

Paragraph 20. The system according to Paragraphs 18 and 19, characterized said fixing ring has the ratio of its outer diameter to its inner diameter in the range of 1.10 to 1.31, wherein its cross-section has any geometry, preferably rectangular with a cross-sectional area in the range of 1.54 square inches to 2.10 square inches, preferably in the range of 1.61 square inches to 1.90 square inches.

Paragraph 21. The system according to Paragraph 8, wherein the upper cap-plug (TC_S) has a hollow hemispherical geometry, with a concave side and a convex side, and an axial symmetry axis, coaxial to the symmetry axis of the main body, having an access, in its central area to house and hermetically fix an outlet pipe (TSA).

Paragraph 22. The system according to Paragraph 21, wherein the access follows the shape and dimensions of the cross section of the outlet pipe, with a flange at the lower end of the upper cap-plug connecting to the upper end of the cylindrical section for disassembly and maintenance and/or inspection of the solids separation module.

Paragraph 23. The system according to Paragraphs 21 and 22, wherein the upper cap-plug (TC_S) is made of materials whose minimum yield strength is 36,000.00 psi, preferably carbon steel.

Paragraph 24. The system according to Paragraphs 21 and 22, wherein the height of the upper cap-plug (TC_S) is in the range of 5.31 inches to 9.54 inches and the ratio of its height to its outer diameter (L_TCS/D_TCS) is in the range of 0.18 to 0.81, wherein its outer diameter and wall thickness are selected equal to the outer diameter and wall thickness of the cylindrical section.

Paragraph 25. The system according to Paragraph 8, wherein the lower cap-plug (TC_I) has a hollow hemispherical geometry, with a concave side and a convex side with an axial symmetry axis, coaxial to the symmetry axis of the main body, having an access in its central area to house and fix on its convex side a solids outlet duct (SS), where its concave side serves as support for the rectangular supports of the impact plate (PIM).

Paragraph 26. The system according to Paragraph 25, wherein the lower cap-plug is hermetically bonded to the lower end of the cylindrical section and is made of materials whose minimum yield strength is 36,000.00 psi, preferably carbon steel.

Paragraph 27. The system according to Paragraphs 25 and 26, wherein the lower cap-plug has a height in the range of 5.31 inches to 9.54 inches and the ratio of its height to its outer diameter (L_TCI/D_TCI) is in the range of 0.18 to 0.81, wherein its outer diameter and wall thickness are selected equal to the outer diameter and wall thickness of the cylindrical Section.

Paragraph 28. The system according to Paragraph 9, wherein the slotted tube (TUR) is a hollow cylindrical element of straight section, whose perimeter shape follows the shape of the cylindrical section of the main body and is concentric to it.

Paragraph 29. The system according to Paragraph 9, wherein the outer diameter of the slotted tube is smaller than the inner diameter of the cylindrical section of the main body and is supported by the fixing ring, is incorporated within the main body, and is mechanically fixed so that it does not rotate with respect to its axial axis or in any other direction.

Paragraph 30. The system according to Paragraph 9, wherein the side wall of the slotted tube (TUR) has a plurality of accesses whose number and distribution are specific patterns or randomly distributed therein, preferably rhombic or polygonal patterns, and more preferably rectangular patterns on the curved surface of the slotted tube.

Paragraph 31. The system according to Paragraph 9, wherein the slotted tube accesses have any shape, preferably cylindrical with an angle of inclination of its longitudinal symmetry axis above a horizontal plane in the range of 13.5 degrees to 17.0 degrees.

Paragraph 32. The system according to Paragraph 31, wherein the distribution of the accesses on the circumference of the slotted tube is every 360/n degrees, these angles measured from the center of symmetry in a cross section, wherein n is an integer lying in the interval from 5 to 12, preferably in the interval from 6 to 10.

Paragraph 33. The system according to Paragraphs 31 and 32, wherein the angle of inclination of the accesses with respect to lines perpendicular to radial lines drawn at every 360/n degrees is in the interval from 13.5 degrees to 17.0 degrees.

Paragraph 34. The system according to Paragraph 9, wherein the space between the outer face of the slotted tube (TUR) and the inner face of the cylindrical section (SC) receives the fluid matrix with solids coming from the inlet tube (TE) and initiates the separation of the solids from the fluid matrix by confining the fluid, increasing its velocity and forcing the separation through the existing accesses in the slotted tube.

Paragraph 35. The system according to Paragraph 9, wherein the slotted tube is fabricated with materials whose minimum elastic limit is 36,000.00 psi, preferably carbon steel, being subject to special treatments to improve its resistance to erosion.

Paragraph 36. The system according to Paragraph 9, wherein the ratio of its outer diameter of the slotted tube to the inner diameter of the cylindrical section of the main body is in the range of 0.72 to 0.95.

Paragraph 37. The system according to Paragraphs 9 and 36, wherein the height of the cylindrical wall of the slotted tube is in the range of 7.20 inches to 9.67 inches without exceeding, the upper end of the cylindrical section of the main body, once it is supported on the fixing ring.

Paragraph 38. The system according to Paragraphs 9, 36 and 37, wherein the wall thickness of the slotted tube is preferably in the range of 0.21 inches to 0.61 inches and more preferably in the range of 0.22 inches to 0.56 inches.

Paragraph 39. The system according to Paragraphs 9 and 30 to 33, wherein the vertical distance between centers of every two adjacent accesses on the slotted tube is equal to H_TUR/t, taken from the horizontal plane (PH), wherein/is in the range of 8.00 to 10.27.

Paragraph 40. The system according to Paragraph 9, wherein the wear sleeves (CD) are a plurality of plates mechanically fixed to the inner wall of the cylindrical section, and are supported on the fixing ring.

Paragraph 41. The system according to Paragraph 9, wherein the wear sleeves are installed adjacent to each other until they cover the entire inner wall of the cylindrical section in the height range of the slotted tube, likewise, they cover the perimeter area of the cylindrical section at the same height of the slotted tube.

Paragraph 42. The system according to Paragraph 9, wherein the wear sleeves are treated to reduce erosion wear.

Paragraph 43. The system according to Paragraph 9, wherein the wear sleeves are made of materials whose yield strength is at least 36,000.0 psi, preferably carbon steel.

Paragraph 44. The system according to Paragraphs 9 and 34, wherein the thickness (t_CD) of the wear sleeves is in the range of 0.07 inch to 0.133 inch.

Paragraph 45. The system according to Paragraphs 9, 34 and 44, wherein the radius of the circular section of the wear sleeves (R_CD) is equal to DI_SC/2, and the angle γ, which is measured at the perimeter of the of the of the wear sleeves is 360º/m, wherein m is an integer, such that the plurality of wear sleeves completely covers the inner wall of the cylindrical section in the height range of the slotted tube.

Paragraph 46. The system according to Paragraphs 9, 34, 44 and 45, wherein the height of each wear sleeve (H_CD) is in the range of 7.20 inches to 9.67 inches.

Paragraph 47. The system according to Paragraph 9, wherein the cylinder-cover (TAC) is a flat plate-shaped element, whose geometry follows the perimeter shape of the cylindrical section of the main body and covers the entire upper area of the slotted tube, except in its central region.

Paragraph 48. The system according to Paragraph 9, wherein the cylinder-cover (TAC) is installed mechanically fixed on the slotted tube and includes in its central region, an access through which the outlet pipe (TSA) passes.

Paragraph 49. The system according to Paragraph 9, wherein the cylinder-cover divides the internal volume of the main body into two regions, a region above the cylinder-cover forming a mechanical-acoustic damping chamber, and another region below it, where solids and liquid matrix are separated and conveyed.

Paragraph 50. The system according to Paragraph 9, wherein the cylinder-cover is treated to reduce erosion wear due to its location on the slotted tube.

Paragraph 51. The solids separation module subsystem, according to Paragraph 9, wherein the cylinder-cover is made of materials whose yield strength is at least 36,000.0 psi, preferably carbon steel.

Paragraph 52. The solids separation module subsystem, in accordance with Paragraphs 9 and 47, wherein the thickness of the cylinder-cover is in the range of 0.20 inches to 0.44 inches.

Paragraph 53. The system according to Paragraph 9, wherein the outlet pipe (TSA) is a hollow elongate element through which the fluid matrix already separated from the granular solids is conducted and connected to the fluid matrix outlet conduit (SMF).

Paragraph 54. The system according to Paragraph 9, wherein the outlet pipe is an element formed of two parts, one upper and one lower, whose cross section has any shape, preferably circular, wherein, its longitudinal axis is collinear with the longitudinal axis of the main body.

Paragraph 55. The system according to Paragraphs 9 and 54, wherein the length of the outlet pipe starts from the lower space of the main body, passes through the slotted tube, the cylinder-cover, the damping chamber and exits through the upper Cap-plug.

Paragraph 56. The system according to Paragraphs 9, 54 and 55, wherein the upper part of the outlet pipe (TSA) is mechanically and hermetically fixed to the upper cap-plug, without any possibility of movement, and the lower part is mechanically coupled to the upper part of the outlet pipe.

Paragraph 57. The system according to Paragraph 9, wherein the outlet pipe is made of materials whose yield strength is at least 36,000.0 psi, preferably carbon steel.

Paragraph 58. The system according to Paragraph 9, wherein the outlet pipe is subjected to special treatments to improve its resistance to erosion.

Paragraph 59. The system according to Paragraphs 9 and 53, wherein the overall length of the outlet pipe is in the range of 29 inches to 35 inches and its outer diameter, is in the range of 1.90 inches to 2.88 inches; and because the ratio of its inner diameter to its outer diameter is in the range of 0.72 to 0.86.

Paragraph 60. The system according to Paragraph 9, wherein the strainer (CED) is a tubular element, preferably cylindrical of straight circular cross-section with a multiplicity of holes in its longitudinal area, which is rigidly and mechanically connected to the outlet pipe at its lowermost end.

Paragraph 61. The system according to Paragraphs 9 and 60, wherein the CED functions as a barrier for finer solid particles, further limiting the number and diameter size of particles that can reach the outlet pipe.

Paragraph 62. The system according to Paragraph 9, wherein the strainer (CED) is subjected to special treatments to reduce its erosion wear and is made of materials whose yield strength is at least 36,000.0 psi, preferably carbon steel.

Paragraph 63. The system according to Paragraph 9, wherein the overall length of the strainer (CED) is in the range of 17 inches to 22 inches and its outer diameter, is in the range of 1.90 inches to 2.88 inches with a ratio of its inner diameter to its outer diameter, in the range of 0.72 to 0.86 and the ratio of the sum of the areas of the holes to its total lateral area is in the range of 0.01 to 0.89.

Paragraph 64. The system according to Paragraph 9, wherein the impact plate (PIM) is a flat plate shaped element with rectangular supports, whose geometry follows the perimeter shape of the bottom cap-plug and is installed and supported on the concave side of the bottom cap-plug by its rectangular supports.

Paragraph 65. The system according to Paragraphs 9 and 64, wherein the design and location of the impact plate under the slotted tube functions both, as a vortex limiter and router towards the outlet pipe, and solids router towards the bottom outlet through the bottom cap-plug and through the periphery of the impact plate.

Paragraph 66. The system according to Paragraphs 9, 64 and 65, wherein the impact plate is treated to reduce erosion wear and is fabricated from materials whose yield strength is at least 36,000.0 psi, preferably carbon steel, with a plate thickness in the range of 0.10 inches to 0.40 inches and a diameter (D_PIM) in the range of 9.50 inches to 10.75 inches.

Paragraph 67. The system according to Paragraphs 9 and 64 to 66, wherein the dimensions of the rectangular supports of the impact plate are such that the ratio of their height h_PPIM, to their length l_PPIM, is in the range of 0.35 to 0.45 and their length is in the range of 11.50 inches to 12.90 inches, while the thickness of the rectangular supports, t_PPIM, is in the range of 0.10 inches to 0.20 inches.

Paragraph 68. The system, of Paragraph 1, wherein conveying the fluid matrix and solids to the outlet of the solids separation module is carried out via two separated outlet piping lines: the solids outlet conduit (SS) and the fluid matrix outlet conduit (SMF).

Paragraph 69. The system according to Paragraphs 9 and 53, wherein the fluid matrix outlet conduit is connected to the upper end of the solids separation module outlet pipe to channel and dispose of the fluid matrix in a controlled manner.

Paragraph 70. The system according to Paragraphs 9 and 53, wherein the fluid matrix outlet conduit (SMF) is a tubular element, preferably cylindrical with a straight circular cross-section, and includes shutoff valves capable of withstanding pressures up to 3,000.0 psi and pressure sensors capable of withstanding pressures up to 5,000.0 psi.

Paragraph 71. The system according to Paragraph 9, wherein the fluid matrix outlet conduit (SMF), is made of materials having a minimum yield strength of 36,000.0 psi, preferably carbon steel.

Paragraph 72. The system according to Paragraph 9, wherein the outer diameter of the fluid matrix outlet conduit is in the range of 2.00 inches to 6.00 inches.

Paragraph 73. The system according to Paragraph 9, wherein the solids outlet conduit (SS) is a tubular, preferably cylindrical element with a straight circular cross-section that is connected to the lower end of the solids separation module through its bottom cap-plug (TC_I) and conveys the separated granular solids in a wet state to the solids collection and monitoring system (FIC).

Paragraph 74. The system according to Paragraphs 9 and 73, wherein the solids outlet conduit (SS) is made of materials having a minimum yield strength of 36,000.0 psi, preferably carbon steel.

Paragraph 75. The system according to Paragraph 9, wherein the solids outlet conduit has an outer diameter in the range of 1.75 inches to 3.00 inches.

Paragraph 76. The system according to Paragraph 9, wherein the solids outlet conduit has pressure sensors capable of up to 5,000.0 psi and shutoff valves capable of withstanding pressures up to 3,000.0 psi.

Paragraph 77. The system according to Paragraph 1, wherein the solids collection and monitoring system (FIC) receives and monitors the already separated solids coming from the main body of the solids separation module and is channeled through the solids outlet conduit.

Paragraph 78. The system according to Paragraph 77, wherein the solids collection and monitoring system includes a main body, an inlet Tube, an outlet pipe and a Strainer incorporated therein.

Paragraph 79. The system according to Paragraph 1, wherein the solids collection and monitoring system receives granular solids in a wet condition through the upper inlet tube to be deposited within the solids collection and monitoring system strainer, which has multiple perforations, such that the remaining fluids are channeled through the lower outlet pipe.

Paragraph 80. The system according to Paragraph 77, wherein the main body of the solids collection and monitoring system (CP_FIC) has cylindrical, spherical, conical, conical, polyhedral or combination thereof geometry, preferably cylindrical-spherical, with a longitudinal symmetry axis.

Paragraph 81. The system according to Paragraph 77, wherein the main body of the solids collection and monitoring system includes an inlet tube (TE_FIC), an outlet pipe (TS_FIC) and a cylindrical section with two terminations, one hemispherical and the other threaded cylindrical.

Paragraph 82. The system according to Paragraph 77, wherein the main body of the solids collection and monitoring system is sized to receive and process granular solids in wet condition.

Paragraph 83. The system according to Paragraph 77, wherein the main body of the solids collection and monitoring system is made of materials having a minimum yield strength of 36,000.0 psi, preferably carbon steel.

Paragraph 84. The system according to Paragraph 81, wherein the ratio of length to outer diameter of the cylindrical section of the solids collection and monitoring system is in the range of 3.25 to 5.10, and preferably in the range of 4.1 to 5.0.

Paragraph 85. The system according to Paragraph 81 and 84, wherein the cylindrical section ratio of its inner diameter to its outer diameter is in the range of 0.82 to 0.91, the inner diameter preferably being between 7.1 inches and 7.9 inches and its thickness being in the range of 0.44 to 0.59 inches.

Paragraph 86. The system according to Paragraph 81, wherein the inlet tube of the solids collection and monitoring system is a hollow tubular element with an axis of longitudinal symmetry forming a right or inclined angle with respect to the longitudinal axis of the main body, preferably forming a right angle, and whose cross section has any geometrical shape, preferably circular, hermetically connected to the cylindrical section of the main body at its upper part.

Paragraph 87. The system according to Paragraph 81, wherein the inlet pipe of the solids collection and monitoring system (TE_FIC) is conduit for conveying the granular solids in wet condition to the main body of the solids collection and monitoring system, and is mechanically rigidly connected thereto.

Paragraph 88. The system according to Paragraph 81, wherein the inlet pipe of the solids collection and monitoring system is made of materials having a minimum yield strength of 36,000.0 psi, preferably carbon steel.

Paragraph 89. The system according to Paragraph 81, wherein the wall thickness of the inlet pipe of the solids collection and monitoring system is in the range of 0.13 inches to 0.42 inches and the ratio of its outer diameter to the outer diameter of the cylindrical section of the solids collection and monitoring system, DE_TEFIC/DE_SCFIC, is preferably in the range of 0.12 to 0.33, and more preferably in the range of 0.17 to 0.33.

Paragraph 90. The system according to Paragraph 81, wherein the outlet pipe of the solids collection and monitoring system is a hollow tubular element with an axis of longitudinal symmetry; it may form a right angle or may be inclined with respect to the longitudinal axis of the main body, preferably forming a right angle, and whose cross section may have any geometrical shape, preferably circular, hermetically connected to the cylindrical section of the main body at its lower part.

Paragraph 91. The system according to Paragraph 81, wherein the outlet pipe of the solid capture and monitoring system (TS_FIC) is a conduit for transporting the remaining liquids, without solids, and to their final disposal, from the main body of the solid capture and monitoring system, and is mechanically rigidly connected to it.

Paragraph 92. The system according to Paragraph 81, wherein the outlet pipe of the Solid Capture and Monitoring System (TS_FIC), is made with materials whose minimum yield strength is 36,000.0 psi, preferably carbon steel.

Paragraph 93. The system according to Paragraph 81, wherein the wall thickness of the outlet pipe of the solid capture and monitoring system is in the range of 0.13 inches to 0.42 inches and the ratio of its outer diameter to the outer diameter of the cylindrical section of the main body, DE_TSFIC/DE_SCFIC, is preferably in the range of 0.12 to 0.33 and more preferably in the range of 0.17 to 0.33.

Paragraph 94. The system according to Paragraph 77, wherein the strainer of the solid capture and monitoring system (CED_FIC) is a hollow tubular element with a multiplicity of holes in its longitudinal area, with a fixing ring in the form of a hoop at its upper end, and a plate that closes its lower end.

Paragraph 95 The system according to Paragraphs 77 and 81, wherein the strainer of the solid capture and monitoring system is located within the main body of the solid capture and monitoring system, supported on the concave side of the lower hemispherical termination of the main body of the solid capture and monitoring system, and is encapsulated within the main body by means of a composite cap screwed onto the upper end.

Paragraph 96. The system according to Paragraph 77, wherein the strainer of the solid capture and monitoring system stores the granular solids already separated of the remaining fluids existing in them.

Paragraph 97. The system according to Paragraph 77, wherein the strainer of the solid capture and monitoring system is made with materials whose minimum yield limit is 36,000.0 psi, preferably carbon steel.

Paragraph 98. The system according to Paragraphs 77, 79, and 94, wherein the length, L_CEDFIC, of the perforated surface of the strainer of the solid capture and monitoring system is in the range of 34.0 inches to 39.0 inches, and its outer diameter is such that the distance between the wall of the inner face of the main body of the Capture and Monitoring System and the outer face of the sieve of the solid capture and monitoring system is 0.75 inches, and the ratio of the sum of the areas of the holes to the total area of the side wall of the sieve of the solid capture and monitoring system is in the range of 0.01 to 0.98.

Paragraph 99. The system according to Paragraph 94, wherein the fixing ring of the strainer of the solid capture and monitoring system (AF_CPFIC), is rigidly and mechanically attached to the upper end of the strainer of the solid capture and monitoring system, and its outer diameter is nominally equal to the inner diameter of the main body of the solid capture and monitoring system.

Paragraph 100. The system according to Paragraph 94, wherein the fixing ring of the strainer of the solid capture and monitoring system allows the insertion and extraction of the strainer, and includes frames made of the same material, which function as reacting elements when the strainer is installed inside the main body and a composite cap is placed on it.

Paragraph 101. The system according to Paragraph 94, wherein the fixing ring of the sieve of the solid capture and monitoring system is made of a material with a minimum yield limit of 36,000.0 psi, preferably carbon steel and treated to withstand erosion wear.

Paragraph 102. The system according to Paragraph 95, wherein the composite cap is formed by a cylindrical coupling element that starts with an inner thread at one end, and ends with a drag stop at the other.

Paragraph 103. The system according to Paragraph 95, wherein the composite cap includes a drag counter cap that makes contact with the drag stop of the coupling element, forming a safety mechanism by reaction, such that the contact pressure between the latter and the frames of the fixing ring of the sieve causes rigid fixation to the main body, as the threaded coupling element advances.

Paragraph 104. The system of Paragraph 95, wherein the composite cap is made of a material with a minimum yield limit of 36,000.0 psi, preferably carbon steel, treated to withstand erosion wear.

Paragraph 105. The system of Paragraphs 1 and 6, wherein the separation of fluids and solids embedded in them, when carried out with a plurality of solid separation modules connected in parallel, wherein the system operates each module independently to increase or reduce the flowrate of solids and fluid separation, and they operation and maintenance is accomplished independently.

Paragraph 106. The system of Paragraphs 1 and 6, wherein the separation of fluids and solids embedded in them, when carried out with a plurality of solid separation modules connected in series, wherein the system allows all modules to operate at the same time to increase the volume of solid separation and reduce, with each added module, the size range of the separated granular solids.

List of abbreviations and acronyms

Abbreviation Description
BPD          Barrels per day
CCD          Classical cyclone design
GLCC         Gas-Liquid Cylindrical Cyclone Separator
             (Gas-Liquid Cylindrical Cyclone)
GSCC         Gas-Solid Cylindrical Cyclone Separator
             (Gas-Solid Cylindrical Cyclone)
LLCC         Liquid-liquid cylindrical cyclone separator
             (Liquid-liquid Cylindrical Cyclone)
GSCS         Gas-solids cyclone separator
             (Gas-solids cyclone separator)
SC           Cyclone separator.
GS           Gas-solids
GL           Gas-liquids
Holdup       Ratio of volume occupied by a liquid flowing in
             a duct section to the volume of the section.

BRIEF DESCRIPTION OF THE DRAWINGS

To give a better understanding of the objects described hereafter, the figures accompanying the present disclosure are described below.

FIG. 1 shows the angle of incidence between the inlet tube and the main body in cyclone separators.

FIG. 2 shows the different conditions of the inlet tubes arriving at the main body of the separator.

FIG. 3 illustrates the mechanism of solid particle wetting in a Venturi device: a) gas access with contaminant particles, b) particle wetting and c) droplets with trapped particles.

FIG. 4 presents a schematic of a disc-based decanter showing a) inlet of the dispersion, b) outlet of the clarified liquid, c) discs and d) separated solids.

FIG. 5 reveals a schematic of a typical screw separator, where: a) is the access of the dispersion, b) the diffraction plate, c) output of solids and d) output of clarified liquids.

FIG. 6 shows the standard configuration of a cyclone separator according to Lapple (Cited by Mahender, 2016).

FIG. 7 shows the schematic representation of a cyclone separator: a) raise view showing the tangential connection of the smaller diameter section known as the inlet tube to the large diameter section (main body), b) external view in the connection area and c) internal view of the connection area between both sections.

FIG. 8 illustrates the shape of the inlet nozzle of the inlet tube to the main body; a) rectangular cross-section and b) circular cross-section.

FIG. 9 shows a chronology of representative dust separator models. this figure is taken from Funk et al. (2013).

FIG. 10 shows the illustration of a particle subjected to a force field inside a typical cyclone separator.

FIG. 11 discloses the geometry of a typical GLCC Separator and its relationship to angular velocity.

FIG. 12 shows the geometry change of a separator from conical section to cylindrical section with vortex limiter, LV.

FIG. 13 illustrates the geometry change of a vortex locator from cylindrical section (a) and slotted conical section (b).

FIGS. 14A-14D show different designs and geometries of gas-solid-liquid separators in cylindrical-spherical separators (Images adapted from Hoffman & Stein, 2007 and U.S. Pat. No. 11,007,542 B2, 2020). FIG. 14A illustrates a conical vortex finder geometry designed to accelerate the flow velocity at the inlet and capture larger volumes of gases and control vortex control and efficiency by raising or lowering the vortex boundary plate. FIG. 14B illustrates a conical vortex finder geometry that includes a blade system within the main body to accelerate higher density molecules and/or particles towards the walls of the main body and get them out through a side outlet at its bottom and, at the same time, control the direction of the vortex carrying lighter molecules. FIG. 14C illustrates a conical vortex finder geometry for the separation of vapors and liquids, others include propellers to graduate the separation speed and stimulate the formation of inverse vórtices. FIG. 14D illustrates a conical vortex finder geometry that uses a plurality of cyclones within a single vessel.

FIG. 15 presents the elements of the first stage which includes access conduits (COA), bypass valves (VAP), pressure sensors (SEP) and flow meters (MGA).

FIGS. 16A-16B illustrate a main body whose shape is hollow cylindrical with two cap-plugs, one upper (TC_S) and one lower (TC_I), both hollow hemispherical. FIG. 16A illustrates an external view of the MSS. FIG. 16B illustrates a longitudinal section of it. FIG. 16 considers the elements of the second stage that integrate one Solids separation module (MSS).

FIG. 17 illustrates the geometrical properties of the Top and Bottom Cap-plugs (TCS and TCI).

FIG. 18 discloses the illustration of the geometrical properties of the Slotted Tube (TUR).

FIG. 19 illustrates the geometrical properties of the Wear Sleeves (CD).

FIG. 20 shows the illustration of the geometrical properties of the Wear Tube (TDES).

FIG. 21 shows the illustration of the geometrical properties of the Impact Plate (PIM).

FIG. 22 discloses the elements of the third stage which includes solids outlet ducts (SS), fluid matrix outlet ducts (SMF), valves (VAP) and pressure sensors (SEP).

FIGS. 23A-23B illustrate an embodiment of a main body of the solids collection and monitoring system (CP_FIC) of the present disclosure. FIG. 23A illustrates an external view of the CP_FIC.

FIG. 23B illustrates a longitudinal section of the same, along with an enlargement of the region indicated in the left part of FIG. 23B. FIGS. 23A-23B consider the elements of the fourth stage that integrate a solids collection and monitoring system (FIC).

FIGS. 24A-24B illustrate the tandem configuration of a plurality of Solids Separation Modules for onshore activities. FIG. 24A illustrates a parallel configuration. FIG. 24B illustrates a series configuration.

FIG. 25 discloses the tandem configuration of a plurality of Solids Separation Modules for offshore activities.

FIG. 26 exhibits the illustration of granular materials of Example 1.

FIG. 27 shows a histogram of the grain-size distribution of a sample from the granular material of Example 1.

FIG. 28 shows the particle size curve based on the number of particles in the sample of Example 1.

FIG. 29 shows the illustration of the trajectory, with arrows and dotted lines, of the two-phase fluid feed consisting of a liquid and granular material, through the equipment of the present disclosure, RESUSS-II-IMP.

FIG. 30 presents the efficiency curve for different flowrates in Example 1.

DETAILED DESCRIPTION

A list of symbols used herein is provided at the end of this section.

Described herein below is a system of the present disclosure for the segregation of production solids in hydrocarbon wells, referred to as a “portable modular apparatus for retaining, diagnosing and measuring of proppant solids in hydrocarbon producing wells”, RESUSS-II-IMP. In accordance with the present disclosure, in certain aspects, this system includes the processes of reception of fluids with solids, separation of solids, analysis of granular solids for the measurement and diagnosis of their production in the targeted well, as well as the equipment for transport and controlled separation of these materials and liquids during the production processes. One objective of its operation is the separation of solids from a fluid matrix, by means of the formation of a helical trajectory, where a vortex is generated around an axis in the direction of gravity. The effect of the vortex and the forces involved is the separation of granular solids from the fluid matrix.

This system includes a solids separation module (MSS), which was developed based on the principle of cyclonic separation to separate solids that are transported in a fluid matrix, subject to high pressures, and comprises the following four stages:

• • 1. First stage; a subsystem of piping, valves, and sensors upstream of the Solids Separation Module inlet.
  • 2. Second stage; a subsystem enabling the separation of solids from the liquid matrix, consisting of a separation apparatus called the “Solids Separation Module (MSS)” of this disclosure, with a Main Body (CP) and the following elements incorporated therein:
    • a. Slotted tube (TUR),
    • b. Wear sleeves (CD),
    • c. Cylinder-cover (TAC),
    • d. Outlet pipe (TSA),
    • e. Strainer (CED),
    • f. Wear Tube (TDES),
    • g. Impact plate (PIM),
    • h. Damping chamber (CAM).
  • 3. Third stage: a subsystem of valves and pipes at the outlet of the Solids Separation Module, which conveys the solids and fluids already separated in different directions.
  • 4. A solids collection and monitoring subsystem.

First Stage Description.

This stage includes the piping, valves and sensors necessary to channel and monitor the full fluid matrix, solids included in it, prior to entry the Main Body and the elements incorporated in it, which comprise the Solids Separation Module described in the second stage.

Prior to the entry of the fluid matrix into a Solids Separation Module, piping, valves and sensors are required to monitor and control the flow into it; as a manner of example of a typical, but non-limiting configuration, a line of these elements may include:

Access conduits (COA). These elements (FIG. 15) are means of conveying the fluid matrix with solids at high pressures from a wellhead or collection head to the Solids separation module (MSS), and are fabricated of materials that withstand high pressures with a minimum yield strength of 36,000.0 psi. Example 1 includes carbon steel piping, with diameters in the range of 2.00 inches to 6.00 inches. These lines have pressure sensors (SEP) of up to 5,000.0 psi measurement range, shut-off valves (VAP) rated to withstand pressures up to 3,000.0 psi, and equipment to measure flow rates up to 10 barrels per minute.

Second Stage Description.

The main body of the apparatus (CP) of the present disclosure, FIG. 16, is a vessel made of materials that withstand high stresses, preferably having a minimum yield strength of 36,100.0 psi. These vessels are sized to receive and process granular solids that are conveyed in a fluid matrix.

The main body can adopt a cylindrical, spherical, conical, polyhedral or combination of them, preferably cylindrical-spherical, with a longitudinal symmetry axis.

For illustrative purposes, Example 1 of a main body, FIG. 16, whose shape is hollow cylindrical with two cap-plugs, one upper (TC_S) and one lower (TC_I), both hollow hemispherical, is presented and illustrated in the same figure. Note that in FIG. 16, the image on the left (FIG. 16A) illustrates an external view of the MSS, and the one on the right (FIG. 16B) a longitudinal section of it. The cylindrical section (SC) of the Main Body indicated in FIG. 16A, has a length to outside diameter ratio (L_SC/DE_SC) in the range of 1.80 and 3.20, preferably between 1.85 and 2.91 with an inside to outside diameter ratio (DI_SC/DE_SC) between 0.81 and 0.99, and an inside diameter (DI_SC) measuring preferably between 7.10 inches and 14.50 inches. The wall thickness depends on the material used to construct it; to illustrate this, in Example 1, the material used is carbon steel and its thickness is in the range of 0.5 to 0.6 inches. In order to disassemble the top cap-plug for inspection, maintenance and/or operation monitoring, the main body has a top flanged connection that hermetically connects the hollow cylindrical section of the CP with the upper cap-plug on its concave side.

Inlet pipe (TE). In this element, illustrated in FIG. 16, the fluid matrix containing the solids is conveyed to the main body, and is preferably connected tangentially to the main body, as illustrated in the same figure; its longitudinal axis may form a right angle or be inclined with respect to the longitudinal axis of the main body. In its cross section, it is designed in circular, rectangular or other geometries, as schematized in FIG. 8. Another feature is that the inlet nozzle to the main body can have a straight or conical section, as featured in FIG. 2. In Example 1 of the present disclosure, a straight circular section pipe is designed, the material of manufacture of which must have a minimum yield strength of 36,000.0 psi, such as carbon steel pipe. The wall thickness of the TE, t_TE, is in the range of 0.21 inches to 0.42 inches, and the ratio of its outside diameter to the outside diameter of the cylindrical section of the CP, DE_TE/DE_SC, is preferably in the range of 0.12 to 0.22, and more preferably in the range of 0.15 to 0.19. The longitudinal axis of the TE, for illustrative purposes in Example 1, forms a 90° angle with respect to the longitudinal axis of the main body of the MSS as illustrated in FIG. 16B and its cross section is circular in its length up to the area where it meets the CP.

Fixing Ring (AF). Inside the main body, in its Cylindrical Section, there is another ring-shaped element, made of a material with a minimum elastic limit of 36,000.0 psi, concentric to the Main Body, called Fixing Ring (AF); this element is mechanically fixed to the inner wall of the Main Body, without any possibility of displacement (FIG. 16B) and works as a simultaneous support for the Grooved Tube (TR), the Wear Sleeves (CD) and the Wear tube (TDES), these last three are incorporated elements described below. The outside diameter of the AF (DE_AF) fits tightly inside the cylindrical section and is nominally equal to the inside diameter of the main body cylindrical section and coaxial to it. This element is located at a height (H_AF) of 1.94 times its outside diameter from the bottom end of the cylindrical section, i.e. H_AF/DE_AF=1.94, as illustrated in FIG. 16. The ratio of the outside diameter to the inside diameter of the fixing ring (AF) is in the range of 1.10 to 1.31.

The AF cross-section can have any geometry, preferably rectangular with a cross-sectional area in the range of 1.54 square inches to 2.10 square inches, preferably in the range of 1.61 square inches to 1.90 square inches.

Upper cap-plug (TC_S). This element, shown in FIGS. 16 and 17, is hermetically bonded to a flange. In Example 1 of the present disclosure, the material used is carbon steel with minimum yield strength of 36,000 psi. The top (TC_S) and bottom cap-plugs (TC_I) have both, hemispherical geometry with an axis of axial symmetry as shown in FIG. 17. The height of the top cap-plug, L_TCS, is in the range of 5.31 inches to 9.54 inches and the ratio of its height to the outside diameter of the top cap-plug (L_TCS/D_TCS) is in the range of 0.18 to 0.81; the external diameter and wall thickness of the cap-plugs are selected equal to the external diameter and wall thickness of the Cylindrical Section. The upper Cap-layer has an access, in its central area, to house and fix a “Vortex Locator”, also identified as “Outlet Pipe” (TSA), which conveys the fluids already separated from the solids; this access follows the shape and dimensions of the cross section of the Outlet Pipe (TSA). The lower cap-plug is connected to the cylindrical section by its concave side in an airtight manner, as shown in FIG. 16.

Lower cap-plug (TC_I). This element, illustrated in FIG. 17, has an access in its central area to house and hermetically fix a discharge pipe on its convex side, which channels the solids already separated from the fluids; the solids outlet duct (SS) is manufactured with a material whose elastic limit is at least 36,000.0 psi. This cap-plug also serves as a support on its concave side for the rectangular supports of the Impact Plate (PIM). The height of the bottom cap-plug, L_TCI, is in the range of 5.31 inches to 9.54 inches and the ratio of its height to the outside diameter of the bottom cap (L_TCI/D_TCI) is in the range of 0.18 to 0.81; the external diameter and wall thickness of the cap-plugs are selected equal to the external diameter and wall thickness of the cylindrical section of the main body. The lower cap-plug has an access, in its central area, to lodge and fix a discharge pipe, which allows channeling the solids already separated from the liquids.

The following is a description of the elements incorporated into the main body.

Slotted Tube (TUR). Unlike separation systems shown in the prior art for the separation of solids from a fluid phase, where the cyclonic separation is by direct jetting on the inner wall of the main body, in the present disclosure a novel separation element has been developed to make more efficient the separation of a fluid matrix and granular solids embedded therein, which is described here. The flow of the fluid matrix with solids, coming from the TE, is conducted in the space formed between the inner face of the Cylindrical Section of the CP and the outer face of the Slotted Tube, confining the fluid, increasing its velocity and forcing the separation through the accesses that the TUR has in its wall. The slotted tube consists of (FIGS. 18a and 18b) a hollow cylindrical structure of straight section, whose perimeter shape follows the shape of the Cylindrical Section of the CP and is concentric to it. The outer diameter of the TUR is smaller than the inner diameter of the CP Cylindrical Section. The space between these two elements receives the fluid matrix with solids coming from the TE and separates the solids from the fluid matrix.

The TUR is made of a high strength material, the yield strength of which is at least 36,000.00 psi. In Example 1 of this present disclosure, carbon steel is used. This element is located within the Cylindrical Section of the Main Body and is supported by the Fixing Ring (AF). The TUR is mechanically fixed so that it does not rotate with respect to its axial axis or in any other direction. The ratio of the outside diameter of the TUR, DE_TUR, to the inside diameter of the Main Body Cylindrical Section, DI_SC, is in the range of 0.72 to 0.95. The height of the cylindrical wall of the TUR, H_TUR, is in the range of 7.20 inches to 9.67 inches without exceeding, once supported on the AF, the top end of the cylindrical section of the CP. The wall thickness of the TUR is preferably in the range of 0.21 inches to 0.61 inches and more preferably in the range of 0.22 inches to 0.56 inches. The TUR includes, in its side wall, accesses, identified as AR in FIG. 18, that receive the fluid matrix containing the granular materials coming from the TE, the number and distribution of these accesses can be in specific patterns or randomly distributed in the wall of the TUR, however, and according to the experiences acquired by the inventors, these accesses are, in Example 1 of the present disclosure, rectangular patterns on the curved surface of the TUR, as shown in FIG. 18. Investigations by the inventors indicate that these accesses are even more efficient when they are cylindrical and their axis of longitudinal symmetry has an angle of inclination, a, above a horizontal plane, PH, indicated by a line, in the range of 13.5 degrees to 17.0 degrees, as shown in the same FIG. 18 in its section (a). In an elevation view as shown in the cross section of in the top image of FIG. 18, the distribution of these accesses on the circumference of the TUR is every 360/n degree, where n is an integer that lies in the interval from 5 to 12.

In Example 1 of the present disclosure, n is equal to 8; the tilting angle β, of the accesses, with respect to lines perpendicular to radial lines drawn at every 360/n degrees, is in the range of 13.5 degrees to 17.0 degrees. The height of the Slotted Tube, H_TUR, is in the range of 7.20 inches to 9.67 inches and the vertical distance between centers of every two accesses is H_TUR/t, taken from the horizontal plane (PH), where t is in the range of 8.00 to 10.27, as indicated in section (a) of FIG. 18. This element is exposed to high erosive forces; therefore, it is required that the TUR be subjected to special treatments to improve its erosion strength.

Wear Sleeves (CD). The space between the Slotted Tube and the Cylindrical Section is designed to receive, from the Inlet Tube, the full flow of the fluid matrix with solids in it; On the other hand, erosion evaluations on the inner face of the Cylindrical Section where it receives this flow, led to the requirement of minimizing the erosion in this section, therefore some Wear sleeves were designed and added (FIG. 19), these are plates mechanically fixed to the inner wall of the cylindrical section of the CP and are also supported on the AF, as indicated in the inset of FIG. 16B. The CDs directly receive energy from the fluid and granular matrix at the outlet of the TE, therefore, they are subject to intense wear and must be hardening-treated to withstand erosion.

In Example 1 of the present disclosure carbon steel is used having a yield strength of at least 36,000.0 psi. Since the CD's cover the perimeter area of the Cylindrical Section at the same height as the TUR, the number of these plates can be from one to a plurality of them, installed adjacent to each other to cover the entire inner wall of the Cylindrical Section, covering the height range of the slotted tube. The thickness of the Wear Sleeves, t_CD, is in the range of 0.07 inch to 0.133 inch, the radius of their circular section R_CD is equal to DI_SC/2 and the angle γ, which subtends the perimeter of the DCs (FIG. 19), is 360°/m, where m is an integer such that the plurality of Wear Sleeves completely and uniformly covers the inner face of the SC in the height interval of the TUR. The height of each CD is in the range of 7.20 inches to 9.67 inches.

Cover-cylinder (TAC). This element covers the TUR entire upper area, except in its central region as indicated below, and consists of a flat element whose geometry follows the perimeter shape of the CP cross-section, and its plate thickness is in the range of 0.20 inches to 0.44 inches. The CT is installed, mechanically fixed, on top of the Slotted Tube (TUR). In its central region the TAC includes an access through which the Outlet Pipe (TSA) passes. The TAC divides in two the interior space of the CP; above the TAC it forms a mechanical-acoustic buffer chamber (CAM) indicated in FIG. 16, and below it the volume where the solids are separated and channeled from the liquid matrix. The TAC, because of its location above the TUR, is subject to intense wear and must be treated to withstand erosion wear. In Example 1 of the present disclosure, the CT is fabricated from carbon steel whose yield strength is at least 36,000.0 psi.

Outlet pipe (TSA). This element, shown in the longitudinal section of FIG. 16, starts from the lower space of the main body, passes through the TUR, the TAC, the CAM and exits through the upper cap-plug. The TSA is typically a hollow cylindrical element, although its cross section may have another shape, whose longitudinal axis is collinear with the longitudinal axis of the main body and allows receiving and channeling the fluid matrix already separated from the solids for its subsequent disposal. This element, because to its location on the TUR, is subject to intense wear and must be treated to withstand erosion wear. The TSA, in Example 1 of the present disclosure, is a cylindrical element of straight circular section, composed of two parts, one upper and one lower.

The upper part of the TSA is mechanically fixed to the TC_S, without any movement, and the lower part is mechanically coupled to the former. The TSA is made of carbon steel, whose yield strength is at least 36,000.0 psi. This element is exposed to high erosive forces and is therefore, required to be subjected to special treatments to improve its resistance to erosion. The overall length of the TSA, LTSA, is in the range of 29 inches to 35 inches and its outside diameter, DE_TSA, is in the range of 1.90 inches to 2.88 inches. The ratio of its inside diameter to its outside diameter, DI_TSA/DE_TSA, is in the range of 0.72 to 0.86.

Strainer (CED). This is a tubular element with a multiplicity of holes in its longitudinal area, which is rigidly and mechanically connected to the TSA at its lower end, as illustrated in FIG. 16B. The CED functions as a barrier for finer solid particles, further limiting the number and size of particles that can reach the outlet pipe (TAS).

The CED, in Example 1 of the present disclosure, is a cylindrical element of straight circular cross-section fabricated from carbon steel whose yield strength is at least 36,000.0 psi and is subject to intense wear so that it must be subjected to special treatments to withstand erosion wear. The overall length of the CED, L_CED, is in the range of 17 inches to 22 inches and its outside diameter, DE_CED, is in the range of 1.90 inches to 2.88 inches. The ratio of its inside diameter to its outside diameter, DI_CED/DE_CED, is in the range of 0.72 to 0.86 and the ratio of the sum of hole areas to the total sidewall area of the CED is in the range of 0.01 to 0.89.

Wear tube (TDES). This element, shown in the longitudinal section of FIG. 16B and FIG. 20, has a flange at its upper end with which it rests on the AF.

The TDES is typically a hollow cylindrical element, although its cross section may have another shape, whose longitudinal axis is collinear with the longitudinal axis of the Main Body and allows to receive and convey-by the effect of gravity, viscous forces and induced centrifugal forces—the solids on its internal surface towards the TC_I in a downward spiral trajectory for their subsequent disposal. Simultaneously the already separated fluid matrix and some lower mass particles accumulate away from the TDES wall and are forced to reverse their flow direction in an upward trajectory around the longitudinal axis of the TDES to exit through the Outlet Pipe (TSA), also known as the “vortex finder”. The Wear tube, because of its functionality and location under the TUR, is subject to intense wear and must be treated to withstand erosion wear.

The TDES, in Example 1 of the present disclosure, is a cylindrical element of straight circular cross-section, fabricated from carbon steel whose yield strength is at least 36,000.0 psi. Its overall upper face-to-lower face length, H_TDES, is in the range of 23.8 inches to 25.9 inches, preferably in the range of 24.60 inches to 25.80 inches. The ratio of its inside diameter to its outside diameter, DI_TDES/DE_TDES, is in the range of 0.89 to 0.98; its inside diameter, DI_TDES, is in the range of 10.10 inches to 10.87 inches; and the ratio of its inside diameter to its flange diameter, DP_TDES, is in the range of 0.72 to 0.89.

Impact Plate (PIM). The Impact Plate is a plate with rectangular supports attached to one side, as shown in FIG. 16B and illustrated in FIG. 21. The PIM is housed and supported inside the lower Cap-layer on its concave side, with its rectangular supports. The geometry of the PIM follows the perimeter shape of the lower cap-plug; because of its location under the TUR, it functions as a vortex limiter and router to the TSA and solids router to the bottom outlet through the lower cap-plug and around the periphery of the PIM. The PIM is subject to intense wear and must be treated to withstand erosion wear.

In Example 1 of the present disclosure carbon steel is used whose yield strength is at least 36,000.0 psi, the plate thickness, t_PIM, is in the range of 0.10 inches to 0.40 inches. The diameter, D_PIM, is in the range of 9.50 inches to 10.75 inches. The dimensions of its rectangular supports are such that the ratio of its height, h_PPIM, to its length, l_PPIM, is in the range of 0.35 to 0.45 and its length is in the range of 11.50 inches to 12.90 inches. The thickness of the rectangular supports, t_PPIM, is in the range of 0.10 inches to 0.20 inches.

Third Stage Description.

This stage includes the piping, valves and sensors required to convey and monitor the solids and fluids already separated in different directions, at the outlet to the Main Body of the Solids Separation Module, and the elements incorporated within it; at the outlet of the Solids Separation Module piping, valves and sensors are required to monitor and control the flow of the fluid matrix already separated from the solids on one side and from the solids on the other. In Example 1 which occupies this description of typical, but non-limiting configuration of these elements include the following:

Fluid matrix outlet conduit (SMF). These elements (FIG. 22) are means of conducting the fluid matrix from the Outlet Pipe (TSA) at the upper end of the Solids Separation Module, and are manufactured with materials that withstand high pressures, with a minimum yield strength of 36,000 psi. 0 psi; for this example, carbon steel pipe is included, having a diameter size in the range of 2.00 inches to 6.00 inches; these lines have pressure sensors (SEP) with capacity up to 5,000.0 psi and valves (VAP) with capacity to withstand pressures up to 3,000.0 psi.

Solids outlet conduit (SS). These elements (FIGS. 16 and 22) are means of conducting solids from the lower Cap-plug (TC_I) at the lower end of the Solids Separation Module and are made of materials that withstand high pressures with a minimum yield strength of 36,000.0 psi. For Example 1 of the present disclosure, carbon steel pipe is included, the diameter of which is in the range of 2.00 inches to 6.00 inches. These lines are provided with pressure sensors (SEP) capable of up to 5,000.0 psi and bypass valves (VAP) capable of withstanding pressures up to 3,000.0 psi, for routing to the solids collection and monitoring system (FIC), also known as a “Basket strainer”, described below.

Fourth Stage Description.

Solids collection and monitoring system (FIC). This stage (FIG. 23) includes the apparatus, piping, valves and sensors necessary to receive and monitor the solids already separated coming from the Main Body of the Solids Separation Module described in the second stage, conveyed through the SS and the elements of the third stage. The FIC receives granular solids in wet condition through the TEFIC inlet pipe, deposits them in the multiperforated element and the remaining fluids are channeled through the TS_FIC outlet conduit.

The main body of the solids collection and monitoring system (CP_FIC) of the present disclosure is a vessel made of materials that withstand high stresses, preferably having a minimum yield strength of 36,000.0 psi. These vessels are sized to receive and process granular solids in a wet condition. The CP_FIC may have cylindrical, spherical, conical, polyhedral or combination geometry, preferably cylindrical-spherical, with a longitudinal axis of symmetry.

For illustrative purposes a CP_FIC is presented in Example 1 of the present disclosure, FIG. 23, whose external shape is hollow cylindrical, with a lower end in hemispherical shape (EI_FIC) and an upper cylindrical end with thread termination (ES_FIC), as illustrated in the same Figure. Note that in FIG. 23, the image on the right (FIG. 23A) illustrates an external view of the CP_FIC, the one in the center (FIG. 23B) a longitudinal section of the same and the one on the left an enlargement of the region indicated. The ratio of the length of the main body cylindrical section, L_CPFIC, to its outer diameter, DE_CPFIC, is in the range of 3.25 to 5.10, preferably in the range of 4.1 to 5.0. The inner to outer diameter ratio of the CP_FIC is between 0.82 and 0.91, and an inner diameter (DI_SCFIC), preferably between 7.1 inches and 7.9 inches. Its wall thickness depends on the material used to construct it for, in Example 1 of the present disclosure, the material used is carbon steel and its thickness is in the range of 0.44 to 0.59 inches.

FIC Inlet pipe (TE_FIC). This element, illustrated in FIG. 23A, transports the solids to the CP_FIC and is mechanically and rigidly connected to it, as illustrated in the same FIG. 23. Its longitudinal axis may form a right angle or be inclined with respect to the longitudinal axis of the main body.

In its cross section, the TE_FIC is designed in circular, rectangular or other geometries, in Example 1 of the present disclosure, a circular section pipe is designed, having a minimum yield strength of 36,000.0 psi, for example, carbon steel pipe. The wall thickness of the TE_FIC, t_TEFIC, is in the range of 0.13 inches to 0.42 inches and the ratio of its outside diameter to the outside diameter of the cylindrical Section CP_FIC, DE_TEFIC/DE_SCHIC, preferably lies in the range of 0.12 to 0.33, and more preferably in the range of 0.17 to 0.33. The longitudinal axis of the TEFIC, for Example 1 of the present disclosure, forms a 90° angle with respect to the longitudinal axis of the main body as illustrated in FIG. 23B and its cross-section is circular along its length up to where it meets the CP_FIC.

FIC Outlet pipe (TS_FIC). This element, shown in FIG. 23, transports the remaining liquids to final disposal, and is mechanically and rigidly connected to the CP_FIC, as illustrated in FIG. 23. Its longitudinal axis may form a right angle or be inclined with respect to the longitudinal axis of the main body, CP_FIC; in its cross section, it is designed in circular, rectangular or other geometries; in Example 1 of the present disclosure, a circular section pipe is designed whose material of manufacture must have a minimum yield strength of 36,000.0 psi, for example, carbon steel pipe. The wall thickness of the TS_FIC, tTS_FIC, is in the range of 0.13 inches to 0.42 inches and the ratio of its outside diameter to the outside diameter of the cylindrical section of the CP_FIC, DE_TSFIC/DE_SCFIC, preferably lies in the range of 0.13 to 0.33, and more preferably in the range of 0.17 to 0.33.

The longitudinal axis of the TS_FIC, for Example 1 of the present disclosure, forms an angle of 90° with respect to the longitudinal axis of the Main Body as illustrated in FIG. 23B and its cross section is circular along its length up to where it meets the CP_FIC.

The elements incorporated within the main body of the solids collection and monitoring system are described below.

Strainer of the solids collection and monitoring system (CED_FIC). This is a tubular element with a multiplicity of holes all over its longitudinal area, which allows a) storing the separated granular solids in its interior and b) the exit of the remaining fluids in them.

The lower end of the CED_FIC rests on the hemispherical termination of the CP_FIC, on its concave side, as illustrated in FIG. 23B; the CED_FIC, in Example 1 of the present disclosure, is a cylindrical element of straight circular cross-section manufactured from carbon steel whose yield strength is at least 36,000.0 psi and is exposed to intense wear so that it must be subjected to special treatments to withstand erosion wear. The overall length of the CED_FIC, L_CEDFIC, is in the range of 34.00 inches to 39.00 inches and its outside diameter, DE_CEDFIC, is such that the distance between the inside face wall of the CP_FIC and the outside face of the CED_FIC is 0.75 inches, and the ratio of the sum of hole areas to the total side wall area of the CED_FIC is in the range of 0.01 to 0.89.

The CED_FIC has at one end a ring-shaped element, made of a material with a minimum yield strength of 36,000.0 psi, concentric to the main body, called Strainer Fixing Ring, AF_CPFIC, which allows easy insertion and removal of the CED_FIC and includes frames as illustrated in the box in FIG. 23B, made of the same material; the lower end of the CED_FIG has a plate that closes it; the strainer fixing ring is rigidly and mechanically attached to the upper end of the CED_FIC, and its outer diameter is nominally equal to the inner diameter of the CP_FIC, as shown in FIG. 23B and in the inset of the same Figure. At the same time, the Strainer fixing ring functions as a reaction element by means of its frames when it is installed inside the CP_FIC and a composite cover is fitted on it, as illustrated in the same figure. The composite cover is formed by a cylindrical coupling element that starts with an inner tread at one end and ends with a drag stop at the other end, it also includes a drag counter-cover that makes contact with the drag stop of the coupling element, forming a safety mechanism by reaction, so that the contact pressure between the latter and the frames of the Strainer fixing ring, causes the rigid fixation of the CP_FIC, as the treaded coupling element advances for tightening.

Description of tandem configuration. Up until now, only one solids separation Module has been described, however, its use can be easily extended to tandem operation. The use of several modules in parallel (FIG. 24A) allows to operate each module independently by means of its own valves and sensors, in such a configuration, it is possible to increase or reduce the flow rate during solids separation and/or to supervise its operation and maintenance independently, by simply opening or closing the access valves of each module. Operation in series (FIG. 24B) allows increasing the volume of separated solids and reducing, with each added module, the particle size, making the separation operation more efficient when required.

List of Symbols Used
Access conduits (COA),
Bypass valves (VAP),
Cylinder-cover (TAC),
Cylindrical section (SC),
Cylindrical section outside diameter (DECS),
Cylindrical section inside diameter (DISC),
Cylindrical section length (LCS),
Damping chamber (CAM),
FIC strainer (CEDFIC),
FIC strainer length (LCEDFIC),
FIC cylindrical section (SCFIC),
FIC cylindrical section external diámeter (DESCFIC),
FIC Inlet pipe (TEFIC),
FIC Inlet pipe external diameter (DETEFIC),
FIC Outlet pipe (TSFIC),
FIC Outlet pipe external diameter (DETSFIC),
Fixing ring (AF),
Fixing ring outer diameter (DEAF),
Flow meters (MGA),
Fluid matrix outlet Conduit (SMF),
Grooved Tube (TR),
Impact Plate (PIM),
Impact plate diameter (DPIM);
Impact plate supports height (hPPIM),
Inlet tube (TE),
Inlet tube inner diameter (DITE),
Inlet tube outer diameter (DETE),
Lower cap-plug (TCI),
Main body (CP),
Outlet pipe (TSA),
Pressure sensors (SEP),
Slotted Tube (TUR),
Solids outlet ducts (SS),
Solids collection and monitoring system (FIC),
Solids collection and monitoring system inlet tube
(TEFIC),
Solids collection and monitoring system outlet pipe
(TSFIC),
Solids collection and monitoring system (FIC),
Solids collection and monitoring system main body
(CPFIC),
Solids separation module (MSS),
Strainer (CED),
Strainer fixing ring (AFCPFIC),
Upper cap-plug (TCS),
Valves (VAP),
Wear Sleeves (CD),
Wear Sleeves thickness (tCD),
Wear Sleeves radii (RCD),
Wear Sleeves height (HCD),
Wear Tube (TDES).

EXAMPLES

To show the best mode of operation of the present disclosure known by the applicant, the following Example 1, related to the portable modular apparatus for the retention, diagnosis and selective surface measurement of formation solids and proppant return in hydrocarbon producing wells after completion is presented, according to the object of the present disclosure described above, and without limiting its technical scope.

Example 1

Statement of the problem. It is required to separate a mixture of a working fluid and particles produced from certain formation, as well as proppant, using the RESUSS-II-IMP equipment. The separation competence of this equipment is to be evaluated in terms of its efficiency to separate the working fluid from the particles in the mixture.

Materials and methods: A sample of these particles was analyzed using image processing techniques and a HA YEAR digital microscope, model HY-10A-T, 5× digital zoom and Panasonic CMOS Sensor 1/2.3″. An image of these particles is shown in FIG. 26. The shiny solid material in this mixture is characteristic of formation materials that have undergone abrasive wear and fracture, as is evident in the rounded shape and smaller amorphous particles of the same material.

The mixture also includes darker, rounded particles whose average diameter is of the order of 500 μm. The latter particles are characteristically well-rounded and resistant proppant granular materials of slightly smaller uniform size than the former. FIG. 27 shows a histogram with the distribution of particle diameter sizes, where a double peak is observed, which makes evident the fracturing of some particles. A statistical analysis of the sample diameter sizes yielded the results shown in Table 2. On the other hand, the working fluid is a water-based fluid with density ρ=1.01 g/cm³ and viscosity of μ=0.000798 kg/(m·s) at an average temperature of 30° C.

FIG. 28 shows a particle size distribution curve of the materials in the sample analyzed, based, on the total number of particles in the sample. It shows that the values defining the uniformity of the sample material are D₁₀=22 μm and D₆₀=84 μm, so the value of the uniformity coefficient is:

$C_u=\frac{D_{60}}{D_{10}}=\frac{84}{22}=3.8$

Sowers & Sowers indicate that materials with Cu<4 are uniform, while those with Cu>6 are well graded materials, if there is symmetry and smoothness in the curve. From the above, it is concluded that the materials studied, also observed in the image in FIG. 26, are relatively uniform in nature in the sample.

TABLE 2
Results of the statistical analysis of diameter sizes
in the sample of Example 1 of the present disclosure.
Sample size = 420.0 particles
Maximum diameter = 1513.9 μm
Minimum diameter = 112.8 μm
Sample mean diameter = 606.9 μm
Sample median = 667.6 μm
Sample mode = 159.6 μm

Separation method. FIG. 29 shows a RESUSS-II-IMP unit with five separation modules, numbered from one (1) to five (5), although the flexibility of the design allows the inclusion of one module or a plurality of them. The two-phase mixture of working fluid and particulates was channeled into the RESUSS-II-IMP unit via the feed flange (denoted at (a) of FIG. 29) to one of the unit modules, as shown below:

• • a) Three samples of granular material (initial weight Wi), whose granulometry and shape description are indicated above, were mixed with the working fluid, creating a two-phase mixture.
  • b) The biphasic mixture with the density and viscosity of the working fluid indicated, was injected into the RESUSS-II-IMP equipment at 30° C. by the piping, whose trajectory is shown with arrows and dotted lines denoted at (b) in FIG. 29, using a DISCFLO boundary layer pump, model 403-14-2HHD with a capacity of 79 GPM at a maximum pressure of 200 psi.
  • c) By opening of valves (denoted at (d) in FIG. 29) the mixture was conveyed to solids separation module number one of the RESUSS-II-IMP in this configuration (denoted at (c) in FIG. 29), although one or several separation modules can be operated simultaneously.

Strategically installed pressure sensors allowed monitoring the pressure in the RESUSS-II-IMP lines throughout the separation process (denoted at (e) in FIG. 29); the photograph denoted at (e) in FIG. 29 shows a pressure sensor at the inlet of separation module number five.

• • d) In order to determine the efficiency of a module, three different flow rates and pressures were used to separate the granular solids from the mixture.
  • e) The efficiency of the separation operation, n_R, in percentage, was evaluated by weighing the solids already separated and accumulated, W_f, in the Solids Collection and Monitoring System, also known as “Basket Filter” (denoted at (f) in FIG. 29) and comparing it with the original weight, Wi, by means of the expression:

${\eta }_R=100-\frac{W_i-W_f}{W_i}·100$

Results. The values of pressure at the inlet of the RESUSS-II-IMP, the flow rate in the inlet line, in barrels per day (bpd), the weight of the sample at the inlet and the weight of the sample at the outlet of the basket strainer and finally the value of the separation efficiency are shown in FIG. 30.

FIG. 30 shows graphically the efficiency of the RESUSS-II-IMP equipment in the separation of the granular samples used in this example.

TABLE 3
Separation efficiency results for the indicated flowrates.
Pressure	Flow rate	Initial weight	Final weight	Efficiency
(psia)	(bpd)	(kg)	(kg)	(%)
18.52	1358.60	22.40	20.95	93.5
23.06	2264.30	22.20	21.30	95.9
28.58	2916.50	22.50	21.60	96.0

Discussion Different criteria have been issued for the measurement of efficiency in cyclone separators, e.g. Fuping Qian et al. (2009), Funk (2013), Funk et al. (2013), Hoffmann et al. (2007) and Kouba et al. (1995).

On the other hand, and since these criteria correlate strongly with particle size, efficiency has also been defined in terms of a “cut-off point” (Funk, 2013) representing the particle size for which 50% separation efficiency is obtained. For diameters greater than 50%, efficiency tends to approach 100%. Each criterion obeys to specific conditions and/or needs and there is no standardization regarding them. Despite the above, the general opinion is that the efficiency of a phase separation equipment is also the result of the optimal combination of the geometry and roughness of the equipment, the nature of the multiphase flow (for example, Shweta, C. et al., 2018, reports very high efficiencies, greater than 98%, in the separation of gases and liquids), the flow and pressure conditions, the nature and geometry of the solid particles, if any, and the interaction between them. However, the criteria to define the efficiency of a cyclone separator are sensibly convergent towards two scenarios: a) separation capacity and b) pressure drops; for this reason, in Example 1 of the present disclosure, a practical and simple criterion oriented towards the separation capacity, as mentioned above, has been chosen.

As can be seen in Table 3, the efficiencies measured during the operation of the RESUSS-II-IMP equipment are above 93%, and reach up to 96%, for the indicated flowrates and pressures, therefore, in terms of separation efficiency in cyclone systems, the separator of the present disclosure is considered to be of high separation efficiency.

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www.researchgate.net/publication/259101451_Dust_cyclone_technology-A_literature_review/download.

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Claims

1. A system for efficient separation of granular solid materials embedded in a fluid liquid matrix from hydrocarbon wells under conditions of high pressure up to 2,000.0 psi and temperatures up to 150° C., comprising: (a) a subsystem for receiving a fluid liquid matrix mixed with solids; (b) a subsystem for the controlled separation of solids embedded in a fluid liquid matrix by means of a solids separation module; (c) a subsystem comprising both the solids outlet conduit and the fluid matrix outlet conduit; (d) a solids capture and monitoring (FIC) subsystem for analysis of the granular solids and measurement and diagnosis of their production in the target well.

2-5. (canceled)

6. The system according to claim 1, wherein the separation of the fluid liquid matrix and the solids embedded therein is carried out with one or a plurality of solids separation modules, each of which includes a main body and a plurality of embodiments.

7. (canceled)

8. The system according to claim 1, wherein the solids separation module subsystem comprises a main body comprising: a) cylindrical section (SC); b) inlet tube (TE); c) fixing ring (AF); d) top cap-plug (TCS); and e) bottom cap-plug (TCI).

9. The system according to claim 1, wherein the solids separation module subsystem comprises the following embodiments: f) slotted tube (TUR); g) wear sleeves (CD); h) cylinder-cover (TAC); i) outlet pipe (TSA); j) strainer (CED); and k) impact plate (PIM).

10-14. (canceled)

15. The system according to claim 8, wherein the inlet tube (TE) is longitudinally hollow and conveys the fluid matrix containing the solids towards the main body (CP), preferably tangentially connected, wherein its longitudinal axis forms a right or inclined angle with respect to the longitudinal axis of the main body, preferably forming a right angle, wherein its cross-section is of straight or conical section, preferably kept straight until rigidly and hermetically joined to the cylindrical section of the main body.

16. (canceled)

17. (canceled)

18. The system according to claim 8, wherein the fixing ring (AF) is in the form of a ring having an inner diameter, an outer diameter and a thickness, and is fixed to the main body (CP) without any possibility of displacement, concentric to it, in its cylindrical section, wherein its outer diameter fits tightly within the cylindrical section and is nominally equal to the inner diameter of the cylindrical section of the main body and coaxial to it, functioning as a simultaneous support for the grooved tube, the wear sleeves and the wear tube.

19-23. (canceled)

24. The system according to claim 8, wherein the upper cap-plug (TCS) has a hollow hemispherical geometry, with a concave side and a convex side, and an axial symmetry axis, coaxial to the symmetry axis of the main body, having an access, in its central area to house and hermetically fix an outlet pipe (TSA), wherein the access follows the shape and dimensions of the cross section of the outlet pipe, with a flange at the lower end of the upper cap-plug connecting to the upper end of the cylindrical section for disassembly and maintenance and/or inspection of the solids separation module, and wherein the height of the upper cap-plug (TCS) is in the range of 5.31 inches to 9.54 inches and the ratio of its height to its outer diameter (LTCS/DTCS) is in the range of 0.18 to 0.81, wherein its outer diameter and wall thickness are selected equal to the outer diameter and wall thickness of the cylindrical section.

25-27. (canceled)

28. The system according to claim 9, wherein the slotted tube (TUR) is a hollow cylindrical element of straight section, whose perimeter shape follows the shape of the cylindrical section of the main body and is concentric to it.

29. (canceled)

30. The system according to claim 9, wherein the side wall of the slotted tube (TUR) has a plurality of accesses whose number and distribution are specific patterns or randomly distributed therein, preferably rhombic or polygonal patterns, and more preferably rectangular patterns on the curved surface of the slotted tube.

31. The system according to claim 9, wherein the slotted tube accesses have any shape, preferably cylindrical with an angle of inclination of its longitudinal symmetry axis above a horizontal plane in the range of 13.5 degrees to 17.0 degrees.

32. The system according to claim 31, wherein the distribution of the accesses on the circumference of the slotted tube is every 360/n degrees, these angles measured from the center of symmetry in a cross section, wherein n is an integer lying in the interval from 5 to 12, preferably in the interval from 6 to 10.

33. The system according to claim 31, wherein the angle of inclination of the accesses with respect to lines perpendicular to radial lines drawn at every 360/n degrees is in the interval from 13.5 degrees to 17.0 degrees.

34. The system according to claim 9, wherein the space between the outer face of the slotted tube (TUR) and the inner face of the cylindrical section (SC) receives the fluid matrix with solids coming from the inlet tube (TE) and initiates the separation of the solids from the fluid matrix by confining the fluid, increasing its velocity and forcing the separation through the existing accesses in the slotted tube.

35. (canceled)

36. (canceled)

37. The system according to claim 9, wherein the height of the cylindrical wall of the slotted tube is in the range of 7.20 inches to 9.67 inches without exceeding, the upper end of the cylindrical section of the main body, once it is supported on the fixing ring.

38. (canceled)

39. The system according to claim 9, wherein the vertical distance between centers of every two adjacent accesses on the slotted tube is equal to HTUR/t, taken from the horizontal plane (PH), wherein t is in the range of 8.00 to 10.27.

40. The system according to claim 9, wherein the wear sleeves (CD) are a plurality of plates mechanically fixed to the inner wall of the cylindrical section, and are supported on the fixing ring.

41. The system according to claim 9, wherein the wear sleeves are installed adjacent to each other until they cover the entire inner wall of the cylindrical section in the height range of the slotted tube, likewise, they cover the perimeter area of the cylindrical section at the same height of the slotted tube.

42-44. (canceled)

45. The system according to claim 9, wherein the radius of the circular section of the wear sleeves (RCD) is equal to DISC/2, and the angle γ, which is measured at the perimeter of the of the of the wear sleeves is 360°/m, wherein m is an integer, such that the plurality of wear sleeves completely covers the inner wall of the cylindrical section in the height range of the slotted tube.

46. (canceled)

47. The system according to claim 9, wherein the cover-cylinder (TAC) is a flat plate-shaped element, whose geometry follows the perimeter shape of the cylindrical section of the main body and covers the entire upper area of the slotted tube, except in its central region.

48. The system according to claim 9, wherein the cover-cylinder (TAC) is installed mechanically fixed on the slotted tube and includes in its central region, an access through which the outlet pipe (TSA) passes.

49-54. (canceled)

55. The system according to claim 9, wherein the length of the outlet pipe starts from the lower space of the main body, passes through the slotted tube, the cylinder-cover, the damping chamber and exits through the upper Cap-plug.

56-59. (canceled)

60. The system according to claim 9, wherein the strainer (CED) is a tubular element, preferably cylindrical of straight circular cross-section with a multiplicity of holes in its longitudinal area, which is rigidly and mechanically connected to the outlet pipe at its lowermost end.

61-67. (canceled)

68. The system, of claim 1, wherein conveying the fluid matrix and solids to the outlet of the solids separation module is carried out via two separated outlet piping lines: the solids outlet conduit (SS) and the fluid matrix outlet conduit (SMF).

69-76. (canceled)

77. The system according to claim 1, wherein the solids collection and monitoring system (FIC) receives and monitors the already separated solids coming from the main body of the solids separation module and is channeled through the solids outlet conduit, and includes a main body, an inlet tube, an outlet pipe and a strainer incorporated therein.

78. (canceled)

79. The system according to claim 1, wherein the solids collection and monitoring system receives granular solids in a wet condition through the upper inlet tube to be deposited within the solids collection and monitoring system strainer, which has multiple perforations, such that the remaining fluids are channeled through the lower outlet pipe.

80. The system according to claim 77, wherein the main body of the solids collection and monitoring system (CPFIC) has cylindrical, spherical, conical, conical, polyhedral or combination thereof geometry, preferably cylindrical-spherical, with a longitudinal symmetry axis.

81. The system according to claim 77, wherein the main body of the solids collection and monitoring system includes an inlet tube (TEFIC), an outlet pipe (TSFIC) and a cylindrical section with two terminations, one hemispherical and the other threaded cylindrical.

82-86. (canceled)

87. The system according to claim 81, wherein the inlet pipe of the solids collection and monitoring system (TEFIC) is conduit for conveying the granular solids in wet condition to the main body of the solids collection and monitoring system, and is mechanically rigidly connected thereto.

88. (canceled)

89. (canceled)

90. The system according to claim 81, wherein the outlet pipe of the solids collection and monitoring system is a hollow tubular element with an axis of longitudinal symmetry; it may form a right angle or may be inclined with respect to the longitudinal axis of the main body, preferably forming a right angle, and whose cross section may have any geometrical shape, preferably circular, hermetically connected to the cylindrical section of the main body at its lower part.

91-93. (canceled)

94. The system according to claim 77, wherein the strainer of the solid capture and monitoring system (CEDFIC) is a hollow tubular element with a multiplicity of holes in its longitudinal area, with a fixing ring in the form of a hoop at its upper end, and a plate that closes its lower end.

95-98. (canceled)

99. The system according to claim 94, wherein the fixing ring of the strainer of the solid capture and monitoring system (AFCPFIC), is rigidly and mechanically attached to the upper end of the strainer of the solid capture and monitoring system, and its outer diameter is nominally equal to the inner diameter of the main body of the solid capture and monitoring system.

100. The system according to claim 94, wherein the fixing ring of the strainer of the solid capture and monitoring system allows the insertion and extraction of the strainer, and includes frames made of the same material, which function as reacting elements when the strainer is installed inside the main body and a composite cap is placed on it.

101. (canceled)

102. The system according to claim 77, wherein the composite cap is formed by a cylindrical coupling element that starts with an inner thread at one end, and ends with a drag stop at the other, such that it makes contact with the drag stop of the coupling element, forming a safety mechanism by reaction, so that the contact pressure between the latter and the frames of the fixing ring of the sieve causes rigid fixation to the main body, as the threaded coupling element advances.

103. (canceled)

104. (canceled)

105. The system according to claim 1, wherein the separation of fluids and solids embedded in them, when carried out with a plurality of solid separation modules connected in parallel, wherein the system operates each module independently to increase or reduce the flowrate of solids and fluid separation, and they operation and maintenance is accomplished independently, and when connected in series, the system allows all modules to operate at the same time to increase the volume of solid separation and reduce, with each added module, the size range of the separated granular solids.

106. (canceled)