阅读说明：本技术 从加氢裂化器料流中动电分离固体粒子 (Electrokinetic separation of solid particles from hydrocracker streams ) 是由 艾维·D·约翰逊 布彭德尔·S·米尼亚斯 杰西卡·维特曼 萨拉·L·约埃 托马斯·布鲁诺 于 2018-06-25 设计创作，主要内容包括：本文提供了用于从加氢裂化器工艺料流中除去固体粒子的动电分离方法。(Provided herein are electrokinetic separation methods for removing solid particles from a hydrocracker process stream.)

1. A method for reducing particulates in a hydrocarbon process stream, the hydrocarbon process stream comprising a hydrocracker feed stream or a hydrocracked product stream and particulates, the method comprising removing at least a portion of the particulates from the hydrocarbon process stream by passing the hydrocarbon process stream through at least one electrokinetic separator (EKS) to form a particulate reduced hydrocarbon stream.

2. The method of claim 1, wherein the hydrocarbon process stream is a feed stream to a hydrocracker.

3. The process of claim 1, wherein the hydrocarbon process stream is a hydrocracked product exiting a hydrocracker.

4. The method of any one of claims 1 to 3, further comprising filtering the particulate-reduced hydrocarbon stream with a sub-micron filter.

5. The method of claim 4, wherein the reduction of particulates de-charges the filter and shortens a regeneration time of the filter.

6. The method of any one of claims 1 to 5, further comprising treating the reduced particulate hydrocarbon stream with a hydrocyclone system or a centrifuge system as a polishing step.

7. The method of any one of claims 1 to 6, further comprising passing the hydrocarbon stream through a hydrocyclone upstream of the EKS, or passing the hydrocarbon stream through a filtration system upstream of the EKS, or even passing the hydrocarbon stream through a centrifuge system upstream of the EKS.

8. The method of any one of claims 1 to 7, wherein the microparticles have an average particle size in a range of about 0.1 microns to about 1 micron.

9. The method of any one of claims 1 to 8, wherein at least 50 wt% of the particulates originate from a hydrocarbon processing catalyst as measured by the hot toluene filtration/washing protocol ASTM method D4807-05.

10. The method of any one of claims 1 to 9, wherein the microparticles comprise particles derived from a catalyst, clay, particles derived from reactor equipment, and particles derived from post-reaction processing prior to the EKS.

11. The method of any one of claims 1 to 10, wherein the EKS comprises at least two opposing electrodes having different potentials applying an electric field, and an EKS medium disposed between the electrodes, wherein the EKS medium comprises fibers, fabrics, sheets, foams, pellets, beads, wires, or a combination thereof.

12. The method of claim 11, wherein the EKS media comprises a fabric and the process stream flows through a channel formed at least in part by the fabric.

13. The method of claim 11, wherein the EKS media comprises pellets made of a material selected from the group consisting of inorganic glasses, ceramics, glass-ceramics, inorganic oxides, and mixtures and combinations thereof.

14. The method of any one of claims 11 to 13, further comprising the step of regenerating the EKS media, such as washing the EKS media by recycling a portion of the reduced particulate hydrocarbon stream to the EKS, thereby removing at least a portion of the particles collected in the EKS media, or washing the EKS media by using a process-compatible wash solution to remove at least a portion of the particles collected in the EKS media.

15. The method of claim 14, wherein the process compatible wash liquid is selected from the group consisting of air, nitrogen, hydrocarbon-containing liquids, and combinations thereof.

16. The method of any one of claims 1 to 15, wherein the particulates are removed in a direction different from a flow direction of the hydrocarbon process stream.

17. A system, the system comprising:

a hydrocracker; and

an electro-kinetic separator (EKS),

wherein the EKS is configured to remove at least a portion of particulates from a hydrocracker feed stream to form a particulate-reduced hydrocarbon stream, and the EKS is configured to feed the particulate-reduced hydrocarbon stream to the hydrocracker.

Technical Field

The present invention relates to an electrokinetic separation process for removing solid particles from a hydrocarbon process stream, such as a feed stream or effluent of a hydrocracker.

Background

One method of increasing the feedstock suitable for the production of fuels and lubricants may be to conduct cracking to convert higher boiling petroleum feeds to lower boiling products. For example, high vacuum gas oils and low vacuum gas oils may be hydrocracked to produce additional lubricant base stock range products.

Base stocks are commonly used in the production of lubricants, such as automotive lubricants, industrial lubricants, and greases. A base oil is defined as a combination of two or more base stocks used in making the lubricant composition. They are also used as process oils, white oils, metal working oils and heat transfer fluids. Finished lubricants consist of two basic components: lubricating base stocks and additives. Lubricating base stocks are a major component of these finished lubricants and contribute significantly to the performance of the finished lubricant. Generally, some lubricating base stocks are used to make a wide variety of finished lubricants by varying the mixture of individual lubricating base stocks and individual additives.

Group III basestocks may also be produced from synthetic hydrocarbon liquids obtained from natural gas, coal, or other fossil resources, group IV basestocks such as poly α -olefins (PAO) are produced by oligomerization of α -olefins such as 1-decene, and group V basestocks include all materials not belonging to groups I-IV, such as naphthenes, polyalkylene glycols (PAGs), and esters.

Hydrocrackers are refinery operations used to upgrade hydrocarbon streams. The process receives feed from a number of sources, some of which contain large amounts of particulates that can have a deleterious effect on downstream product specifications, as well as cause equipment corrosion and plugging. Thus, the feed and/or products to the hydrocracker need to be filtered or centrifuged to remove particulates before or after the hydrocracker/hydrotreater. Alternatively, the feed to the hydrocracker may be limited to those having a low particle count.

In addition to the desired lubricant range petroleum products, the process stream exiting the hydrocracker may also contain solid particles (particulates) derived from the catalyst, reactor equipment and reactants. Even if included in a lubricant base stock product at low concentrations, the solid particles can impair, if not reduce to acceptable levels, the properties of the final product. For example, it is known that solid particles contained in lubricant base stocks, if at unacceptable levels, can cause visual clouding or clouding of the final lubricant composition formulated from the base stock, increase the formation of deposits in the lubricant, reduce filterability of the lubricant, reduce its lubricating efficacy, and increase surface corrosion and surface wear of lubricated components, resulting in shortened life of the lubricant and higher risk of premature failure of lubricated equipment or higher energy consumption.

Historically, the particle-containing hydrocracker process feed stream and/or effluent (hydrocracked product) has been passed through one or more stages of mechanical filtration or centrifugation to at least partially remove the solid particles contained therein. Mechanical filtration may include passing the reaction product through a porous membrane having pores that are small enough to exclude a portion of the solid particles. However, the filtration rate can be adversely affected by a number of factors, such as: viscosity of the reaction product, amount of solids to be removed, and/or morphology of the solids. Reducing the filtration time can increase throughput and enable the use of more highly particulate contaminated feed in the process.

Porous membrane filtration generally requires the use of a filter aid, typically in the form of diatomaceous earth, which forms a layer on the membrane filter to help collect solids that would otherwise bypass or clog the filter. After filtration, the filter aid forms a "filter cake" on the surface of the membrane filter along with solid particles in the process stream. The filter cake will absorb liquid product from the product stream. It is wasteful to directly discard the filter cake with the absorbed liquid product; while recovering the absorbed liquid product requires additional materials and steps. The tradeoff between particle filtration rate and degree of partial removal results in at least a portion of the solid particles, particularly those particles having a particle size smaller than the pore size of the membrane, passing through the membrane and becoming entrained in the process stream after filtration.

A process that removes solid particles from a hydrocracker process stream at a faster rate than conventional filtration techniques and/or reduces the amount of solid particles that need to be removed by conventional filtration would be advantageous.

Disclosure of Invention

It has been found that electrokinetic separation ("EKS") can be used to effectively reduce solid particles, even those of particularly small size, from a hydrocracker process stream without or in addition to filtration or centrifugation. The collected solid particle-laden EKS media may be conveniently regenerated in situ or ex situ to restore the particle abatement capability of the utilized EKS, or in some cases may be discarded and replaced with fresh EKS media.

Accordingly, in one aspect, the present invention provides a method for reducing particulates in a hydrocarbon process stream, the hydrocarbon process stream comprising a hydrocracker feed stream or a hydrocracked product stream and particulates, the method comprising removing at least a portion of the particulates from the hydrocarbon process stream by passing the hydrocarbon process stream through at least one electrokinetic separator (EKS) to form a particulate reduced hydrocarbon stream.

In one form, the hydrocarbon process stream is a feed stream for a hydrocracker.

In one form, the hydrocarbon process stream is a hydrocracked product exiting a hydrocracker.

In another form, the method may further include filtering the particulate-reduced hydrocarbon stream with a sub-micron filter.

Advantageously, the reduction in particulates de-charges the filter and shortens the time to regenerate the filter.

In another form, the method may further include treating the particle-reduced hydrocarbon stream with a hydrocyclone system or a centrifuge system as a polishing step.

Additionally, the method may further comprise passing the hydrocarbon stream through a hydrocyclone upstream of the EKS, or passing the hydrocarbon stream through a filtration system upstream of the EKS, or even passing the hydrocarbon stream through a centrifuge system upstream of the EKS.

In another form the microparticles have an average particle size in a range of 0.1 microns to 10 microns.

In yet another form at least 50 wt% of the particulates are derived from a hydrocarbon processing catalyst.

In another form, the particulates include catalyst-derived particles, clays, reactor equipment-derived particles, and particles derived from post-reaction processing prior to EKS.

In yet another form, the EKS includes at least two opposing electrodes having different potentials to apply an electric field, and an EKS medium disposed between the electrodes, wherein the EKS medium includes fibers, fabrics, flakes, foams, granules, beads, wires, or combinations thereof.

Advantageously, the EKS media comprises a fabric and the process stream flows through a channel formed at least in part by the fabric.

Alternatively, the EKS media comprises pellets or beads made of a material selected from the group consisting of inorganic glasses, ceramics, glass-ceramics, inorganic oxides, and mixtures and combinations thereof.

In another form, the method further comprises the step of regenerating the EKS media, such as by washing the EKS media by recycling a portion of the particulate-reduced hydrocarbon stream to the EKS to remove at least a portion of the particles collected in the EKS media, or by washing the EKS media with a process-compatible wash solution to remove at least a portion of the particles collected in the EKS media.

In one form, the process compatible scrubbing liquid is selected from the group consisting of air, nitrogen, hydrocarbon-containing liquids, and combinations thereof.

Advantageously, the particulates are removed in a direction different from the direction of flow of the hydrocarbon process stream.

Other embodiments, including certain aspects of the embodiments outlined above, will be apparent from the detailed description that follows.

Drawings

The drawings described herein are for illustrative purposes only of selected embodiments and not all possible implementations, and are not intended to limit the scope of the present disclosure.

Fig. 1A and 1B schematically illustrate an EKS including fabric EKS media operating in a cleaning mode.

Figure 2 schematically illustrates an EKS including glass beads as EKS media operating in a cleaning mode.

Corresponding reference characters indicate corresponding parts throughout the several views of the drawings.

Detailed Description

The present application describes an alternative or complement to filtration of hydrocracker process streams that reduces particle counts regardless of particle size.

Definition of

The words and phrases used herein should be understood and interpreted to have a meaning consistent with the understanding of those words and phrases by those skilled in the relevant art. No special definition of a term or phrase, i.e., a definition that is different from the ordinary and customary meaning as understood by those skilled in the art, is intended to be implied by consistent usage of the term or phrase herein. To the extent that a term or phrase is intended to have a special meaning, i.e., a meaning other than the broadest meaning as understood by skilled artisans, such a special or explicit definition will be expressly set forth in the specification in a definitional manner that provides the special or explicit definition for the term or phrase.

For example, the following discussion contains a non-exhaustive list of definitions for several specific terms used in the present disclosure (other terms may be defined or clarified elsewhere herein in a defined manner). These definitions are intended to clarify the meaning of the terms used herein. The terms are considered to be used in a manner consistent with their ordinary meaning, but for clarity the definitions are still specified herein.

One/one: the articles "a" and "an" as used herein mean one or more when applied to any feature in the embodiments and implementations of the invention described in the specification and claims. The use of "a" and "an" does not limit the meaning to a single feature unless a limitation is specifically stated. The terms "a" or "an" entity refer to one or more than one of the entity. Thus, the terms "a", "an", "one or more" and "at least one" may be used interchangeably herein.

About: as used herein, "about" refers to the degree of deviation based on the usual experimental error for the particular property identified. The magnitude provided by the term "about" will depend on the particular context and the particular nature, and can be readily discerned by one skilled in the art. The term "about" is not intended to expand or limit the extent to which equivalents of the specified values may otherwise be provided. Moreover, unless otherwise indicated, the term "about" shall expressly include "exactly," consistent with the following discussion regarding ranges and numerical data.

And/or: the term "and/or" disposed between a first entity and a second entity refers to one of: (1) a first entity, (2) a second entity, and (3) the first entity and the second entity. Multiple elements recited with "and/or" should be interpreted in the same manner, i.e., "one or more" of the elements so combined. In addition to the elements specifically identified by the "and/or" clause, other elements may optionally be present, whether related or unrelated to those elements specifically identified. Thus, as a non-limiting example, when used in conjunction with open-ended language such as "comprising," reference to "a and/or B" may refer in one embodiment to a alone (optionally including elements other than B); in another embodiment, only B (optionally including elements other than a); in yet another embodiment, refers to both a and B (optionally including other elements). As used herein in the specification and claims, "or" should be understood to have the same meaning as "and/or" as defined above. For example, when spacing items in a list, "or" and/or "should be interpreted as being inclusive, i.e., including at least one of a plurality of elements or a list of elements, but also including more than one, and optionally other unlisted items. Only terms explicitly indicated to the contrary, such as "only one" or "exactly one", or "consisting of … …" when used in the claims, will indicate that exactly one element of a plurality or list of elements is included. In general, the term "or" as used herein, when preceded by an exclusive term such as "one of either", "one", "only one", or "exactly one", should be understood merely as indicating an exclusive alternative (i.e., "one or the other but not both").

Comprises the following steps: in the claims, as well as in the specification, all transitional phrases such as "comprising," "including," "carrying," "having," "containing," "involving," "holding," "including," and the like are to be understood to be open-ended, i.e., to mean including but not limited to. As described in the us patent office patent inspection program manual, section 2111.03, only the transition phrases "consisting of … …" and "consisting essentially of … …" should be closed or semi-closed transition phrases, respectively. Any device or method or system described herein may include, may consist of, or may consist essentially of any one or more of the elements described.

The range is as follows: concentrations, dimensions, amounts, and other numerical data may be presented herein in a range format. It is to be understood that such a range format is used merely for convenience and brevity and should be interpreted flexibly to include not only the numerical values explicitly recited as the limits of the range, but also to include all the individual numerical values or sub-ranges encompassed within that range as if each numerical value and sub-range is explicitly recited. For example, a range of about 1 to about 200 should be interpreted to include not only the explicitly recited limits of 1 and about 200, but also to include individual sizes such as 2, 3, 4, etc., and sub-ranges such as 10 to 50, 20 to 100, etc. Similarly, it should be understood that when numerical ranges are provided, such ranges are to be construed as providing literal support for claim limitations that only recite the lower value of the range as well as claim limitations that only recite the upper value of the range. For example, a disclosed numerical range of 10 to 100 provides literal support for a claim reciting "greater than 10" (without an upper bound) and a claim reciting "less than 100" (without a lower bound). In the drawings, like numerals designate the same or similar structures and/or features; and each illustrated structure and/or feature may be discussed in detail herein without reference to the figures. Similarly, each structure and/or feature may not be explicitly labeled in the figures; and any structure and/or feature discussed herein with reference to the figures may be used with any other structure and/or feature without departing from the scope of the present disclosure.

Herein, "mechanical filtration" refers to a filtration method for separating solid matter from a solid/fluid mixture, which is achieved only by conventional mechanical forces generated by gravity, centrifugal force, pressure gradient (vacuum or positive pressure), etc., and combinations thereof, without intentionally applying an external force to the solid matter to be separated from the liquid by an electric field. Vacuum assisted drum filters are a widely used mechanical filtration device for separating solids from liquids.

As used herein, "hydrocracking" generally refers to a catalytic process that cracks long hydrocarbon chains into shorter hydrocarbon chains to yield more useful products. A number of patents disclose hydrocracking processes, such as U.S. patent No. 9,499,752, which is incorporated herein by reference in its entirety.

Lubricant base stock manufacture typically begins with a relatively high boiling hydrocarbon fraction, such as light vacuum gas oil (LGO) or heavy vacuum gas oil (HGO) extracted from a vacuum distillation column in a refinery. During processing, the LGO or HGO material is typically subjected to several different catalytic processes to change its composition and/or remove certain impurities. Invariably, at least some particulates, such as catalyst fines or scales (scales) from upstream processing equipment, may enter the hydrocarbon process stream of the hydrocracker. Also, since the hydrocracker itself is a catalytic unit, catalyst fines from the hydrocracker may be entrained in the hydrocracked product, i.e. the effluent of the hydrocracker. Conventionally, the removal of particulates is carried out by mechanical filtration by passing the hydrocarbon process stream through one or more filtration membranes before passing the hydrocarbon process stream to the hydrocracker.

The time, equipment, and process conditions required for filtration to the desired particle count level can be affected by a number of factors, including but not limited to the viscosity of the process stream and the amount of solid particles to be removed. The particulates intended for removal typically accumulate in the mechanical filter to form a "filter cake," which also contains the liquid of the desired product. The filter cake can be disposed of directly with the liquid contained therein, resulting in a waste of a portion of the desired product and unreacted reactants. Alternatively, the filter cake can be washed with a washing liquid to recover the liquid entrained therein. Since mechanical filtration equipment and processes require the use of filtration membranes with limited pore size, it is possible that even after multiple stages of mechanical filtration, certain solid particles, especially those having a size smaller than the pores of the filtration membrane, cannot be completely removed.

Accordingly, the present disclosure addresses these issues by providing a particulate abatement process for hydrocracker feedstocks and/or hydrocracked products, collectively referred to as hydrocracker fluids, using an electrokinetic separator device ("EKS"). In this discussion, electrokinetic separation is defined as a filtration process that captures particles entrained in a hydrocracker fluid according to electrokinetic, dielectrophoretic, and/or electrophoretic principles and produces a hydrocracker fluid with a reduced particle count. The EKS may be placed upstream of the hydrocracker or downstream of the hydrocracker, or both. It may be advantageous if the EKS unit is placed in a slipstream of hydrocracker fluid so that it processes only a portion of the total fluid volume.

One example of an EKS device suitable for use with the process streams of the present application is depicted in fig. 1A and 1B, which is an EKS including fabric EKS media operating in a cleaning mode, and fig. 2 is an EKS including glass beads as EKS media operating in a cleaning mode.

Separation is performed by applying a voltage to electrodes separated by a dielectric to create an electric field. A Direct Current (DC) or Alternating Current (AC) voltage may be applied to the electrodes. The hydrocracker fluid flows through the generated electric field and solid particles, such as catalyst particles, with a charge or polarized charge distribution can move in the desired direction in the electric field, attach to the dielectric and be fixed according to coulomb's law. The end result is that the hydrocracker fluid exiting the EKS contains a reduced amount of particulates.

The vast majority of the particulates contained in the process stream treated by the process of the present invention may originate from the solid catalyst upstream of the hydrocracker. For example, the weight percent of the particulates in the fresh process stream entering the EKS provided by the upstream equipment may range from a 1% to a 2%, where a1 and a2 may be independently 80, 85, 90, 95, 96, 97, 98, 99, 100, as long as a1< a2, based on the total weight of the particulates entrained in the fresh process stream.

The microparticles may have an average particle size of from about 0.1 to about 10 micrometers (μm), for example from about 0.1 to about 1 μm, or from about 0.1 to about 0.5 μm, or even from about 0.1 to about 0.2 μm, as measured by the hot toluene filtration/washing protocol ASTM method D4807-05.

In certain variations, the temperature of the process stream may be adjusted to a desired level by a heat exchanger prior to entering the EKS to optimize the viscosity of the process stream undergoing electrokinetic separation. Thus, it is contemplated that the process stream entering the EKS may have a relatively high temperature.

The EKS may be used in conjunction with a conventional mechanical filtration device. In such embodiments, the EKS is preferably located downstream of the at least one mechanical filtration device, although it may be advantageous to place the EKS upstream of the mechanical filtration device. The EKS is able to capture very fine particles passing through the filter membrane of a mechanical filtration device, so there is an advantage to placing the EKS downstream of a conventional mechanical filtration device.

The EKS includes at least two electrodes made of electrical conductors capable of conducting electricity under operating conditions. The electrodes may be made of any such conductor, such as carbon, silicon, metals and metal alloys (e.g., aluminum, copper, silver, gold and other noble metals, conductive ceramics, etc.).

During operation, a voltage is applied to the electrodes, thereby creating an electric field between the electrodes. The process stream is allowed to pass through the electric field, typically in the direction of the interrupted electric field. The charged solid particles are forced to move in the electric field due to coulomb forces exerted on them. Neutral solid particles can be induced to become electrically polarized in an electric field and then move in a particular direction due to coulomb forces.

The amplitude of the applied voltage and the characteristics of the voltage profile (e.g., constant DC, alternating sine waves, alternating flat pulses, or other profiles), the type of electrode material, the shape, size, and location of the electrodes, and the distance between the electrodes can be selected by one skilled in the art to meet the needs of a particular method of the invention: flow rate of the fresh feed stream, operating temperature, particle concentration in the fresh feed stream, number of EKSs used, desired particle concentration of the stream flowing to downstream equipment, and the like.

Further, as described above, the EKS may include a dielectric medium ("EKS medium") disposed between electrodes that apply an electric field. Suitable EKS media contemplated herein include any solid material having low electrical conductivity under the operating conditions of EKS. Preferably, the EKS medium has a lower electrical conductivity than the electrode material. Preferably, the EKS media has a conductivity that is lower than the process stream fluid at operating conditions. Non-limiting examples of suitable EKS media include fibers, fabrics (e.g., non-woven or woven, cellulose, etc.), sheets, foams, pellets, beads, or wires made from materials such as glass, ceramic, glass-ceramic, inorganic oxides, cellulosic materials such as wood, and combinations and mixtures thereof. In one embodiment, the EKS media may be a fabric, such as a non-woven fabric. The fabric may at least partially define channels of any suitable geometry through which process stream fluid may flow. As the process stream flows through the channels and the electric field, the solid particles can be attracted to the fabric, adhere to the fabric, and be collected on the fabric without being carried to downstream equipment, thereby achieving a particle abatement effect.

In various aspects, the EKS may be operated at a pressure of from about 100kPaa (kilopascal absolute) to about 3500, or from about 100kPaa to about 3000kPaa, or from about 100kPaa to about 2500kPaa, or from about 100kPaa to about 2000kPaa, or from about 100kPaa to about 1500kPaa, or from about 100kPaa to about 1000kPaa, or from about 100kPaa to about 500kPaa, or from about 250kPaa to about 3500kPaa, or from about 250kPaa to about 3000kPaa, or from about 250kPaa to about 2500kPaa, or from about 250kPaa to about 2000kPaa, or from about 250kPaa to about 1500kPaa, or from about 250kPaa to about 1000kPaa, or from about 250kPaa to about 500kPaa, or from about 500kPaa to about 3500kPaa, or from about 500kPaa to about 500kPaa, or about 500 kPaa.

As discussed herein, the treated stream exiting the EKS has a reduced particle content compared to the fresh stream entering the EKS. In various aspects, the treated product stream can comprise solid particles at a concentration of less than about 10,000ppmw (parts per million by weight), less than about 7,500ppmw, less than about 5,000ppmw, less than about 2,500ppmw, less than about 1,000ppmw, less than about 750ppmw, less than about 500ppmw, less than about 250ppmw, less than about 100ppmw, less than about 75ppmw, less than about 50ppmw, less than about 25ppmw, less than about 10ppmw, less than about 1.0ppmw, or less than about 0.50ppmw or about 0.010ppmw, as measured by ASTM D4807-05, based on the total weight of the process fluid exiting the EKS. Additionally or alternatively, the treated product stream can comprise solid particles in a concentration of from about 0.010ppmw to about 10,000ppmw, from about 0.010ppmw to about 5,000ppmw, from about 0.010ppmw to about 1,000ppmw, from about 0.010ppmw to about 100ppmw, from about 0.010ppmw to about 50ppmw, from about 0.010ppmw to about 10ppmw, or from about 0.010ppmw to about 1.0 ppmw.

The EKS may be advantageously used in process streams containing small sized solid particles, such as those having an average particle size of up to 1 micron (μm), such as less than 0.2 μm or 0.1 μm.

As the process stream flows through the EKS, the EKS media may reach a desired level of capture particulates, e.g., any suitable amount, up to a maximum capacity of the EKS media for capturing and retaining solids. This desired capacity of the EKS may be determined by a number of factors including, but not limited to, the voltage profile applied to the electrodes, the flow rate of the process stream, the particle density and particle size distribution in the process stream, the type and capacity of EKS media used to collect the solid particles, and the like.

When the EKS media reaches its particle collection capacity, it may be desirable to regenerate the EKS media to remove at least a portion of the collected particulates from the EKS media, thereby restoring or restoring at least a portion of the capacity. One contemplated regeneration process includes removing contaminated EKS media from an EKS device, cleaning the media using mechanical, chemical, electrical means, and combinations thereof, and reinstalling the thus cleaned media into the EKS device. Solvents, detergents, flames, oxidants, plasmas, brushes, agitation devices, irrigation fluids, and the like may be used to clean the contaminated EKS media.

Alternatively, an in situ regeneration process is used, wherein the EKS medium can be allowed to remain in the EKS device during regeneration. In such an in situ regeneration process, the process stream supply to the EKS may be partially or completely shut off, and the voltage applied to the EKS electrodes may be reduced to zero or changed to a profile that facilitates release of the captured particles so that they may be flushed out of the EKS. During in situ regeneration of the EKS media, a process compatible fluid is passed through the EKS as a backwash, thereby washing out at least a portion of the particulates collected in the media. The process compatible fluid may be any suitable fluid (including liquids, gases, and mixtures thereof), including but not limited to: air, nitrogen, hydrocarbons (e.g., methane, ethane, butane, hexane, cyclohexane, etc.), or solvents. Preferably, the process-compatible wash solution is fluid-miscible with the process stream.

Where the hydrocracking product stream is supplied as a backwash to the EKS to remove at least a portion of the particulates collected therein, at least about 1% to about 20% or about 5% to about 10% of the treated hydrocracking product stream may be recycled through the EKS to collect the deposited particulates. After exiting the EKS, the backwash may be further passed to a separation system (e.g., a mechanical filter, settling tank, EKS, or other separation device) to remove particulates therefrom. The backwash liquid thus recovered can be used for all suitable purposes.

Additionally or alternatively, the EKS media may be replaced instead of being regenerated once it reaches a desired level of captured particles as described herein. For example, the EKS media may be replaced after one separation cycle, two separation cycles, three separation cycles, four separation cycles, or five separation cycles. For example, a first separation cycle may include passing a specified volume of the process stream through the EKS to produce a treated hydrocracker process or product stream, and a second cycle may include passing at least a portion of the treated hydrocracker process or product stream through the EKS, and so on. Alternatively, the first separation cycle may include passing a first specified process stream volume through the EKS to produce a first treated hydrocracker fluid, and the second cycle may include passing a second specified process stream volume through the EKS to produce a second treated hydrocracker fluid.

Alternatively, a continuous fresh feed stream supplied from a facility upstream of the EKS is passed through the EKS to obtain a reduced particulate stream, which is then divided into at least two streams, one of which is recycled to the EKS and the other of which is passed to a downstream facility, which may be a downstream EKS, hydrocracker, distillation column, storage unit, or other vessel. The ratio of the weight of the stream recycled to the EKS to the weight of the fresh feed stream entering the EKS may vary significantly depending on the concentration of particles in the fresh feed stream entering the EKS, the efficiency and capacity of the EKS, and the desired concentration of particles in the stream allowed to flow to downstream equipment. Desirably, the recycle ratio may be in the range of r1 to r2, where r1 and r2 may be independently 0.1, 0.2, 0.3, 0.4, 0.5, 0.6, 0.7, 0.8, 0.9, 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 20, 30, 40, 50, 60, 70, 80, 90, 100, as long as r1< r 2. The higher the recycle ratio, the lower the concentration of particulates in the stream passing to downstream equipment, given that the EKS capacity and efficiency, and all other process conditions, remain equal.

Multiple EKS units may be used, connected in parallel or series or both, to meet the solid particle abatement performance requirements of the process. Preferably, at least two of the plurality of EKS units are configured such that they are capable of operating in parallel, i.e., both receive fresh streams from the same upstream device. A system capable of operating multiple EKS units in parallel achieves the feasibility of operating one EKS in a clean mode (i.e., a mode that receives a fresh feed stream and produces a treated product stream) and one EKS in a regeneration mode or, if desired, an idle mode, thus allowing the entire product manufacturing system to operate stably and uninterruptedly.

The present invention may be used in systems and methods for producing a reduced particle hydrocarbon stream without the need to use any filtration equipment other than EKS. Alternatively, as discussed above, the EKS may be used in conjunction with other filtering devices, such as conventional mechanical filter devices. Although it is preferred that the EKS be downstream of a conventional mechanical filter, it is contemplated that in some instances, a mechanical filter may be installed and used downstream of the EKS. The upstream EKS may reduce the particulate load applied to the downstream mechanical filter, thereby reducing the particulate burden on the filter and shortening the regeneration time of the filter.

The methods described herein can also include a step of processing the reduced particulate hydrocracking product stream with a hydrocyclone system or a centrifuge system as a polishing step. In another form, the hydrocracker feed stream may pass through a hydrocyclone, or a filtration system, or even a centrifuge system, upstream of the EKS.

The particulates released from the EKS during regeneration may be suitably recycled to the hydrocracker. Thus, for this purpose, especially when the backwash contains hydrocracking products, the wash stream comprising process-compatible backwash may be recycled directly to the hydrocracker. In some cases, it may be desirable to separate the solid particles from the fluid in the wash stream in a settling tank or other device, and then recycle the stream enriched in solid particles to the hydrocracker at high loadings. Recycling the particles released from the EKS to the hydrocracker may be particularly advantageous to the extent that the solid particles collected by the EKS contain primarily solid particles originating from the hydrocracker.