Patent Application
20240400911
The present disclosure relates generally to processes, systems, and methods for degumming, bleaching, and/or drying lipid-containing compounds. In particular, some implementations may relate to systems processing of lipid-containing compounds for fuel feedstock through degumming and adsorptive bleaching/drying.
Lipid-containing compounds (LCC) are important raw materials in various industries such as food, pharmaceuticals, fuels, and cosmetics. They can be obtained from natural sources such as animal fats, vegetable oils, and marine oils. However, these sources often contain impurities such as gums, pigments, and other undesirable substances that need to be removed before the lipid-containing compounds can be used in further processing.
Degumming and bleaching processes are methods for purifying lipid-containing compounds. Degumming conventionally involves the removal of gums and other impurities using water and chemical treatment. Bleaching, on the other hand, is conventionally a process of adsorbing pigments and other impurities using a range of adsorptive materials including activated earth, carbon or silica. Conventional methods of degumming and bleaching are typically optimized for single feedstocks, and have been optimized for a narrow range of feed properties. Further, degumming and bleaching have been historically performed to make lipid-containing compounds useful for human consumption. With the increase in lower grade feedstocks for use in energy and fuel, there is a need for more flexible processes that can process a wider range of feedstocks, and optimize products for energy use rather than human consumption.
There is, therefore, a need for an improved process and system for degumming and bleaching lipid-containing compounds that is more efficient, cost-effective, and results in minimal loss of valuable components of the lipid-containing compounds.
In general, one aspect disclosed features a process for treating a lipid containing compound (LCC), the process comprising: producing a first mixture by mixing an aqueous chelate with the LCC, wherein the aqueous chelate comprises Ethylenediaminetetraacetic acid (EDTA), and wherein the LCC is a rendered fat; and separating an aqueous gum containing phase of the first mixture from a lipid containing phase of the first mixture.
Embodiments of the process may include one or more of the following features. In some embodiments, the LCC comprises at least one of: beef tallow; fish oil; algal oil; yellow grease; brown grease; white grease; poultry fat; and hog fat. In some embodiments, the LCC has a free fatty acid content of more than 2% on an oleic acid basis. Some embodiments comprise producing a substantially degummed LCC by treating the lipid containing phase with an adsorbent material. In some embodiments, the substantially degummed LCC has a free fatty acid content above 2%, and a phosphorus content below 3 ppm. Some embodiments comprise vacuum-drying the lipid containing phase prior to treating the lipid containing phase with an adsorbent material. Some embodiments comprise removing spent adsorbent material from the lipid containing phase.
Some embodiments comprise adjusting the pH of the lipid containing phase by adding an acid or base. Some embodiments comprise adjusting the pH of the lipid containing phase to between 3 and 7. Some embodiments comprise breaking emulsions by adding salt to the lipid containing phase. In some embodiments, the salt is sodium chloride or sodium sulfate. In some embodiments, the aqueous chelate further comprises at least one of: sodium salts of EDTA; potassium salts of EDTA; and polymers containing carboxylic acids.
In general, one aspect disclosed features a process for treating a lipid containing compound (LCC), the process comprising: producing a first mixture by mixing an aqueous chelate with the LCC; separating an aqueous gum containing phase of the first mixture from a lipid containing phase of the first mixture; and producing a substantially degummed LCC by treating the lipid containing phase with an adsorbent material, wherein the substantially degummed LCC has a free fatty acid content above 2%, and a phosphorus content below 3 ppm.
Embodiments of the system may include one or more of the following features. In some embodiments, the LCC is a rendered fat. In some embodiments, the LCC comprises at least one of: beef tallow; fish oil; algal oil; yellow grease; brown grease; white grease; poultry fat; and hog fat. In some embodiments, the LCC has a free fatty acid content of more than 2% on an oleic acid basis. Some embodiments comprise producing a substantially degummed LCC by treating the lipid containing phase with an adsorbent material. Some embodiments comprise vacuum-drying the lipid containing phase prior to treating the lipid containing phase with an adsorbent material. Some embodiments comprise removing spent adsorbent material from the lipid containing phase. Some embodiments comprise adjusting the pH of the lipid containing phase by adding an acid or base. Some embodiments comprise adjusting the pH of the lipid containing phase to between 3 and 7. Some embodiments comprise breaking emulsions by adding salt to the lipid containing phase. In some embodiments, the salt is sodium chloride or sodium sulfate. In some embodiments, the aqueous chelate comprises at least one of: Sodium salts of EDTA; Potassium salts of EDTA; and Polymers containing carboxylic acids.
Some embodiments comprise producing a further substantially degummed LCC by treating the lipid containing phase of the first mixture with a further aqueous chelate after the separating and prior to treating the lipid containing phase with an adsorbent material. In some embodiments, a pH of the substantially degummed LCC is different from a pH of the lipid containing phase of the first mixture. In some embodiments, a pH of the substantially degummed LCC is approximately neutral; and a pH of the lipid containing phase of the first mixture is approximately the same as the pKa of phosphaditic acid. In some embodiments, a pH of the substantially degummed LCC is approximately the same as the pKa of phosphaditic acid; and a pH of the lipid containing phase of the first mixture is approximately neutral. In some embodiments, a pH of the substantially degummed LCC is 5-7; and a pH of the lipid containing phase of the first mixture is 3-4. In some embodiments, a pH of the substantially degummed LCC is 3-4; and a pH of the lipid containing phase of the first mixture is 5-7.
The technology disclosed herein, in accordance with one or more various embodiments, is described in detail with reference to the following figures. The figures are provided for purposes of illustration only and merely depict typical or example embodiments of the disclosed technology. These figures are provided to facilitate the reader's understanding of the disclosed technology and shall not be considered limiting of the breadth, scope, or applicability thereof. It should be noted that for clarity and ease of illustration, these figures are not necessarily made to scale.
The figures are not intended to be exhaustive or to limit the invention to the precise form disclosed. It should be understood that the invention can be practiced with modification and alteration, and that the disclosed technology be limited only by the claims and the equivalents thereof.
As biofuel mandates increase, and the demand for low carbon intensity fuels also increases, there is a need to provide robust technologies to convert bio-origin and waste feedstocks into feedstocks that may be converted to useful substances such as fuels.
Historically, the main fuel product from lipid containing materials has been Biodiesel. Biodiesel is comprised of methyl esters, and it substantially different than the hydrocarbon products it replaces. This leads to blending limits, storage incompatibility, an inability to transfer fuel by pipeline and an inability to replace key fuel products such as aviation fuel. When lipid containing materials are subjected to refinery based hydroprocessing to deoxygenate triglyceride and free fatty acid molecules to produce an analog to a hydrocarbon fuel, for example such as diesel and kerosene, the resulting product is a hydrocarbon that is indistinguishable from petroleum derived products. This renewable diesel or jet fuel can then be used in existing infrastructure, and used at higher blend rates, up to and including 100% renewable products.
Historically, triglyceride treatment methods have been tailored to edible oil refining. While the processes and basic chemistry can be leveraged for improving feedstocks for hydroprocessing, the needs of edible oils and hydrotreating units are quite different. Edible oil processing focuses on shelf stability, taste, and color. Biodiesel feedstock preparation is largely focused on reducing free fatty acid content. Refinery hydrotreaters are not impacted by taste or smell. However, very small concentrations, as low as 1 part-per-million, of contaminants such as phosphorous can poison hydrotreating catalysts, dramatically reducing run life and increasing processing cost. Since phosphorous is an integral part of the “gums” of phospholipids that naturally occur in all triglyceride feedstocks, removal of them is essential.
Renewable fuels such as renewable diesel and sustainable aviation fuel that are derived from lipids using conventional middle distillate hydrotreating technology are highly susceptible to premature failure and short catalyst run lengths due to fouling from the contaminants within the renewable feedstocks that are not adequately removed using existing technologies. Premature catalyst failures and shortened operating cycles from fouling are expensive for renewable diesel and sustainable aviation fuel refiners due to the high-costs associated with the changeout of catalysts, which require substantial operating unit downtime, replacement of expensive catalysts, and low-margin transitional periods during startup and shutdown.
These middle distillate hydrotreating technologies often employ a trickle-bed reactor patterned after petroleum refining using a ratio or circulating hydrogen of 3-10 times the hydrogen chemically consumed in converting the feedstock and operating at pressures of 600 psi to 2600 psi and temperatures of 600 F to 750 F. Trickle bed reactors in renewable diesel and sustainable aviation fuel service often use nickel and molybdenum catalysts. These catalysts are solid media with activated metal sites supported by an alumina substrate. Metals, including phosphorus containing compounds, iron, magnesium, sodium, and calcium (either as compounds or elements), are naturally occurring in both plant and animal-derived lipid feedstocks. These metals can cause rapid fouling of the catalyst, even when found in trace volumes (e.g., as low as 1-10 parts per million). In particular, phosphorus-containing compounds can foul catalysts through (1) forming a thin layer of phosphoric glass over the surface of the catalyst which in turn deactivates the active metal sites and also impedes the chemical reaction between the active metals sites and the catalyst's alumina support layer, and (2) causing permanent plugging of open spaces within the catalyst which are irreversible and lead to rapid catalyst deactivation.
Renewable diesel and sustainable aviation fuel processing is intensive, with 11-12% of the feedstock oxygen, the balance being carbon and hydrogen. All oxygen is removed during processing and converted to carbon monoxide, carbon dioxide, and water through decarboxylation and deoxygenation reactions followed by hydrogen saturation of double bonds and hydrogen saturation of some oxygen to form water. In order to initiate the catalytic reactions listed above, a minimum threshold of heat must be introduced to a mixture of feedstock plus hydrogen in conjunction with pressure prior to the introduction of the feedstock to the catalyst bed. These operating conditions require highly specialized pumps, compressors, heat exchanger vessels, reactors, separators, and post-treatment equipment. The extreme operating conditions often are met by constructing this equipment with advanced metallurgy including austenitic stainless steels (e.g., 304, 316, 317, and 347), chrome alloy steels, and high-temperature steels. Many of these metals are susceptible to rapid failure from trace contaminants, particularly organic chlorides, which are found in renewable diesel and sustainable aviation fuel feedstocks.
Typical treatment of edible oil is performed in purpose-built facilities, usually with a single, well-defined feedstock (e.g., soybean oil). As a result, these operating units do not normally have the flexibility to process more than one type of oil. Furthermore, only one degumming step is employed as that is sufficient to refine edible oils. Higher FFA content (e.g., 4%-20% FFA content) is not normally processed in these facilities.
Conventional treatment of edible oils generally involves crude degumming, acid degumming, alkali refining, water washing, drying, bleaching, and deodorizing. Crude degumming involves intensively mixing the crude oil with water, and then centrifuging to remove the most easily hydratable phospholipids within the water phase, leaving a partially degummed oil in the lipid containing phase. Acid degumming involves adding an acid, typically phosphoric or citric acid, to lower the pH and to extract calcium and magnesium from the phospholipids to make the refractory phospholipids hydratable. An alternative is using a strong chelate like EDTA to perform “soft” degumming in lieu of citric or phosphoric acid.
Alkali refining involves pH adjustment of the added acid and any free fatty acids in the oil, and centrifuging to generate a clean oil and a waste stream including soapstock (free fatty acids in a form complexed with an alkali metal, typically sodium). Alternatively, alkali refining may involve only partial neutralization without removing free fatty acids.
Water washing involves washing the clean oil with hot water to remove any entrained acid, alkali or water, followed by centrifugation. Drying involves removing any water from the oil, typically with gentle heating under vacuum to evaporate residual moisture. Bleaching generally involves adding an adsorbent clay to remove any remaining impurities, then removing the adsorbent clay via filtration. Deodorizing involves removing any remaining compounds using a distillation step, focused on removal of volatile compounds in the oil.
Conventional commercial vegetable oil degumming and bleaching processes suffer from the several disadvantages. These processes typically result in a phosphorous level no lower than 3 parts per million, and as high as 10 parts per million. For human consumption, this level of phosphorus is generally undetectable and presents little concern. In a hydroprocessing unit, 3 parts per million of phosphorus will cause catalyst deactivation within 6 to 12 months (versus 4-8 years for hydrocarbon processing). 10 parts per million of phosphorus will cause accelerated catalyst deactivation within weeks after startup. The disclosed processes enable removal of phosphorus to below 1 part per million, and often achieve a “Non-Detect” reading from sensitive laboratory equipment that can measure to the 0.1 ppm level.
Removing the free fatty acids with alkali refining creates a waste stream. For edible oils with <1% free fatty acids, this waste stream is small. For many highly acidic oil streams like those derived from rendered poultry and pork fat, the free fatty acid content can be as high as 20%, resulting in a massive waste stream and impaired yields.
Current commercial processes are not designed to process multiple feedstocks within the same equipment, where gum content, free fatty acid content, and other contaminants may vary by orders of magnitude. Attempting to use a soybean oil degumming and bleaching production line for poultry fat would lead to several limits on throughput, yield, product quality, and depending on the quality of construction and materials choses, could pose metallurgical issues as well.
Embodiments of the disclosed technologies provide a robust, flexible process that is designed to reduce gums, metals, and other contaminants across of a wide range of lipid-containing compounds such as plant- and animal-derived oil feedstocks. These technologies utilize a multi-step process that is more intense than most edible oil processing, ensuring that sufficient treatment is possible with a wide range of feedstocks.
Further embodiments may adopt conventional degumming and bleaching technology and processes to produce improved and otherwise more efficient lipid-containing compound processing. However, as discussed, conventionally, for edible oil production, it is permissible for substances to contain 3-10 ppm phosphorus content in the finished product. While this does not tend to interfere with flavor or color of the oil, the phosphorus plugs and deactivates hydrotreating unit fixed bed catalysts. Additionally, it has been found that phosphorus contents higher that 1 ppm will degrade RD/SAF yields and shorten the expected run time of a hydrotreater's catalyst. As such, disclosed embodiments may produce significantly cleaner substances—one that approaches zero phosphorus and below 3 ppm total metals content.
Present embodiments provide a new approach to RD/SAF feedstocks and have largely solved the long-standing issues troubling the RD industry including short catalyst deactivation periods, reactor fouling, yield degradation, metallurgical mismatches especially as they relate to corrosion attacks on austenitic stainless steels, and logistics and handling issues present in conventional process design.
In general, present embodiments degum and bleach lipid-containing compounds by decanting, water washing (with acids and bases to react with certain compounds), optionally chelating with EDTA, centrifuging, vacuum drying, and filtering with assistance of a bleaching earth. It is the sequencing and the repetition of various processing steps that may result in a higher quality degummed and bleached lipid-containing compound.
The present embodiments include up to three cascaded steps for the separation of metal-contaminated water and clean product oil using disk stack centrifuges.
Solids and other insoluble substances find their way into raw feedstock through a number of means—including for seed oils, the original crushing and flaking process, contamination through handling and shipping, and contamination paths linked to storage. The removal of these coarse and fine contaminants may be completed through basket filtration and physical separation via a horizontal centrifuge. A countercurrent scroll may operate within the centrifuge's bowl to push solids to a discharge port. The cleaned or decanted oil may proceed to a clean oil discharge port. Due to the slower speed of the centrifuge relative to a disk-stack centrifuge, the quality of the separation between phases may not be perfect, but operational experience has shown that most solids will be removed. In addition, a small addition of water can help remove hydratable phosphatide gums, which may form a viscous layer that commingles with the heavier solids and is discharged.
Embodiments of the present disclosure may include two decanters located at the front end of the process.
Embodiments of the present disclosure contemplate the processing of both vegetable oils and animal fats in parallel processing units. In some embodiments, with two discrete degumming lines and two discrete bleaching plants, the process can operate on both types of feedstocks in parallel and optimize the processing conditions for each feedstock. Examples of the raw feedstock qualities are presented below:
Once the lipid-containing compounds have passed through the various disclosed processes the end-product may be a deep degummed and super-bleached renewable diesel plant feedstock. Renewable diesel hydrotreaters require a much deeper level of contaminant removal than do the edible oil and animal feed meal industries. High-pressure hydrotreating equipment has been developed conventionally by the petroleum refining industry that is highly susceptible to trace-level contaminants causing shortened production lives for fixed bed catalysts. In particular, trace remnants of phospholipids (from 2-10 ppm) can foul and deactivate hydro processing catalysts and reduce expected catalyst run lengths by 30-90% versus analogs of petroleum-based oil feedstocks. Given that the costs of a typical catalyst changeout (plus the opportunity cost of downtime) can exceed $20 million per instance, the economic penalty of feed that contains catalyst poisons cannot be undercounted when identifying renewable diesel feedstocks. In addition, higher reactor weighted-average-bed-temperatures in order to offset the catalyst activity rates may become impaired by the phosphorus-compound poisoning, which may further cause significant yield deterioration over the life of the catalyst. The economic losses from this yield slippage can be greater than the economic penalty from short intervals for catalyst changes. The comparison between the needs of current modern hydrotreating equipment and the market for edible refined oils may be exemplified below.
Additionally, for lipid containing oils for human consumption, free fatty acid content (FFA) should be reduced to very low levels, well below 1%. For use in renewable diesel production, these free fatty acids can be a useful feedstock, and it may be useful to both process feedstocks of high (>2%) free fatty acid that would not normally be used in foods, as well as retaining the free fatty acids in the finished product. Thus the ability to remove metals, gums and other contaminants while simultaneously retaining FFA is valuable for renewable diesel feedstocks.
The disclosed embodiments may account for processes that start with either vegetable oil, animal oil, or other fatty substances, and result with an end-product of similar quality. The end-product targets may have most, if not all, impurities removed, in the finished substance. This may provide the end-user with a feedstock or substance that may be compatible with legacy processing equipment. Furthermore, production run times may be comparable to current Ultra Low Sulfur Diesel and Ultra Low Sulfur Kerosine hydrotreater run lengths, thus allowing for a continuation of current maintenance, turnaround, and catalyst replacement methodologies in the refining world.
Phospholipids can enter raw oil through the crushing, flaking, and extraction processes for seed oils. For animal-based greases and tallows, soft tissues are deconstructed through steam and heat in a process known as rendering that liberates fats. Soybeans, for example, are crushed or flaked and then have their oil extracted through a hexane solvent.
It is the solvent extraction process, especially with deep recovery of crushed oil, in which the phosphorus-containing compounds enter the seed oil. If one were to extract 100% of recoverable oil, the phospholipids would be fully mobilized and be well above 1000 ppm phosphorus content in the raw product. With extraction of 99% of the available oil in the soybean, it is common to have phosphorus content in the 500-1000 ppm range.
Phospholipids are complex molecules containing phosphorus, often another metal including magnesium or calcium, and a carbon chain (the lipid). The complexity of these molecules allows them to carry out many functions within biology. They are especially important in the wall structures of cells, functioning as membranes. Hence, these molecules have chemistries that are resistant to many forms of industrial processing.
After physical filtration, vegetable oil and grease pretreatment may commence with water degumming. Phospholipids that can be extracted via a simple water wash are classified as Hydratable Phospholipids. Conversely, those phospholipids not hydratable are termed Non-Hydratable Phosphatides or “NHP” for short. There are generally not hard rules on NHP formation due to the complex interactions of the phospholipids in oil and water phases in addition to other metals and compounds.
Phospholipids can be generally categorized into 4 groups—Phosphatidylcholine (PC), Phosphatidylethanolamine (PE), Phosphatidylinositol (PI), and Phosphatidic Acid (PA). The PC is fully hydratable even when bound to an alkali metal ion, such as potassium, or an alkaline earth metal ion, such as calcium or magnesium. It may also entrain other phosphatides. PI is also fully hydratable. PE is hydratable in the presence of other hydratable phosphatides. After water degumming, some PE may be left in the oil and further water degumming does not remove this PE. PA is hydratable when ionized, but not when neutral or as a calcium or magnesium salt.
The first-stage water wash process may remove more than 75% of the phospholipids as the majority of them are hydratable. Multistage water washes may remove additional contaminants until reaching the limit where only NHPs remain. At this point, additional refining steps may be taken. Conceptually, NHP can be extracted into a water phase when faced with a strong chelate that has a much stronger bond with metals such as Calcium, Magnesium and Iron. It is important to note that the chelate containing water phase usually must make direct contact with the phospholipid and typically only the interface between oil and water can provide a location for the extraction of the NHP. Hence it is relevant for chelate degumming to have a comprehensive dispersion of water into the lipid containing phase (thus forming an emulsion). For the NHP to migrate to the water phase, typically the NHP must be charged after removal of the bound metal. Thus, it is critical that the pH of the solution be above the pka of the phospholipid, thus requiring a pH of approximately 3 or greater. Since the ease of transfer of the phospholipid to water, the binding strength of the chelate/metal complex and the stability of the emulsion are all pH dependent, the ability to control pH for both the chelate/metal binding and separation of aqueous/lipid phases is critical.
Some of the success of the refining process comes from an efficient formation of an emulsion and the ability to separate the phospholipid with that water phase from the product. Hence, mixing speed, residence time, and separation through decanting and mechanical separation via centrifuging are focused on, as opposed to the process chemistry.
The purpose of the refining process equipment is to provide an environment that enables the process conditions to speed up to levels useful for industrial chemistry. The relevant process variables to be controlled during the degumming process include the extent of the water/acid distribution, adequate time being provided at the correct temperature for degumming reactions to occur, and then thorough breaking of the water-in-oil emulsion combined with precision separation in the centrifuges, among others.
When done correctly, the end results can be a nearly perfectly degummed (and de-metaled crude when agents like EDTA are used) oil that is ready for the bleaching process.
The process 300 may feed the water treated mixed oil to Chemical Mixing stage(s) 312 where an acid is added to the water treated oil mixture. The mixture is mixed vigorously through an inline dynamic high-shear mixer, and inline fed to a subsequent stage. Alternatively, other mixing methods such as flow-through restriction via an inline static mixer or aggressive agitation may be used. The acid added may be phosphoric acid that is added to the oil based on the level of phosphorus in the oil. Additional water typically is added during this stage. The total concentration of acid in water (including water added in the prior step) may vary from about 10-30%. Alternatively, other acids such as citric, oxalic, tartaric or other organic acids with some chelating ability may be added. Depending upon the oil being treated, acidity of the water phase is typically within a range of pH 1 to 3.5. For optimal removal of NHP, particularly phosphatidic acid (PA), a pH lower than the pKa of PA (approximately 2.6) is desired.
The material is then fed to a pH adjustment Reactor 314, where the acid/oil mixture is maintained for a period of time while continuing to be agitated and/or stirred to assure complete contact and to allow hydration to occur. This contact stage can last for a few minutes up to several hours. However, the acid/oil mixture continues to be stirred, recirculated or otherwise agitated to avoid settling or separation and ensure continued contact and interaction between the surface area of microbubbles of water and the oil/acid mixture formed during the mixing stage to cause the reaction to move the phosphorus out of the lipid containing phase and into the water phase. For example, the inline process may include optionally an additional shear mixer implementing a recycle loop to avoid settling and to keep the water droplets in the oil/acid mixture small and dispersed throughout the oil/acid mixture. In this pH adjustment stage 314 the acid treated oil mixture is fed to an inline stir tank and is mixed with the addition of an alkali substance, such as sodium hydroxide or with an acid such as phosphoric acid. The sodium hydroxide mixing partially neutralizes the water phase causing a change in the pH of the water phase to between about 4-7. The inline mixing during this pH adjustment stage is not vigorous like in the Chemical Mixing Stage(s) 312. Other alkali substances may be used, such as ammonium hydroxide or potassium hydroxide. Similarly, alternative processing may raise the pH to above neutral to remove free fatty acids (FFA) in feedstocks with FFA content below about 3%. Water may optionally be added to the mixture to allow a larger volume of liquid to remove contaminants in a subsequent stage (e.g., from 5-10% by volume of the oil). To avoid a significant amount of soapstock production, the optimal pH is well below the pKa of the free fatty acids (FFAs). Likewise, to assure complete removal of hydrated gums, the pH is above the pKa of PA. Thus the pH is maintained from about 2.5 to 7 for optimal processing. Further, salts such as Sodium Sulfate and Sodium Chloride can be added in this stage to help reduce the stability of emulsions and improve downstream separation.
The adjusted pH oil mixture is fed to a centrifuge separator 316 (Centrifuge 1) in degumming to remove the water phase and gums 318 from the oil/water mixture. The separated waste water and gums 318 are sent to waste treatment.
The partially degummed oil is fed to a second Reactor 320 (Reactor 2) where the partially-degummed oil is optionally mixed with a chelating substance 322, such as ethylenediaminetetraacetic acid (EDTA) and sodium and potassium salts of EDTA, to further hydrate phospholipids for removal. The amount of EDTA added may typically be from 1-3 times the amount needed stoichiometrically based on remaining iron, calcium and magnesium. The EDTA is an aqueous solution, which may have a total amount of water from 2-5% volume basis related to the oil. Other chelate substances may be used, including a wide range of polycarboxylic acids and polymers. Optionally, the solution of EDTA may be a different salt (e.g., potassium). The EDTA solution may optionally be pH adjusted with an organic acid such as citric acid. In some implementations, a salt, such as Potassium Chloride, Potassium Sulfate, Sodium Chloride, or Sodium Sulfate, may optionally be added to limit the formation of emulsions.
In a second Centrifugation state 324 (Centrifuge 2) the chelate-mixed oil is centrifuged to remove the water phase 326. The removed water may contain the majority of the remaining gums.
The lipid containing phase may be fed to a third reactor 328 (Reactor 3). Water, from 2-5% relative to the lipid containing phase, may be added to wash the lipid containing phase prior to being fed into the inline centrifuge separator in the third centrifuge stage 332 (Centrifuge 3) where the water phase 334 is removed. Additionally, further chemical additives 330 may be added in this stage, for example such as chelating materials. Acid and base may be used to pH adjust the aqueous phase.
The double-cleaned oil may be fed to a vacuum flashing vessel 336 and/or a drying reactor 338, where it is subject to inline dehydrating at vacuum to remove essentially all remaining water with a target of 0.1-0.3%. The pressure of the mixture may be reduced to around 500 millimeters of mercury on an absolute scale. The mixture may be heated to 200 to 210 degrees F. and held for 10 to 40 minutes. The vacuum can be achieved by a vacuum system 440, which generates a vacuum via a vacuum pump, steam ejector or similar process.
The vacuum can be achieved by a vacuum system 340, which generates a vacuum via a vacuum pump, steam ejector or similar process.
The dried oil may be fed to one or more Bleaching Reactors 342 following the vacuum drying, where the oil may be combined with an adsorbent material, for example such as bleaching clay ranging from 0.2% to 0.5% clay to the volume of oil. Other adsorbents such as silicas, activated carbon or finely powdered aluminas may also be used to address specially-required chemical actions including the removal of organic chlorides and sodium. The adsorbent is typically added at a rate of 0.2% to 0.5% of the total feed volume and held in residence while being agitated for 10 to 40 minutes. Other materials, such as filter aids, may be added to ease later recovery. The oil may then be sent to Bleaching Filters 346, where the oil may be filtered through a deep-cake Neutsche-type filter, a pressurized leaf filter or other types of filters (e.g., pressurized candle filters) in order to remove the adsorbent and any adsorbed contaminants.
The filtration may be aided by a filter precoat system 348, which deposits a filter aid on the filtering elements, using materials such as polymers, diatomaceous earth or other filter aids. This helps assure that all adsorbent is recovered and removed from the lipid containing substances.
The purified oil may be stored, at product storage 352, until delivery to customers, at 354.
Some embodiments feature a two-stage degumming process. In these embodiments, the first degumming stage uses a traditional phosphoric acid treatment followed by partial neutralization and centrifugation. The first degumming stage is followed by a second degumming stage using chelates. In some examples, the chelate is Ethylenediaminetetraacetic acid (EDTA).
This two-stage process may remove essentially all phosphorous (via phospholipids). Additionally, having two stages that are each able to remove a large amount of phospholipid provides a large amount of flexibility. Most edible oil facilities process one type of oil continuously. The disclosed technologies may process multiple types of oil. For example, a plant implemented process may handle animal fat one day, then corn oil the next and soy the following, and all are waste products with a lot more variability than an edible oil. These variabilities may include phospholipids, potassium, magnesium, sulfur, nitrogen, metals contamination levels, viscosity, and sediments in the feed oil. Each feed oil has different behavior, and in the event of an issue (e.g., the first stage forms emulsions and a lot of phospholipid gets carried over), there is the ability to complete degumming with the second stage.
The liquid oil is pumped into a Decanter Centrifuge Stage 406 where deionized water is added to the oil and mixed via an inline static mixer to ensure water distribution throughout the oil. Sufficient mixing is performed to assure contact of oil and water, but typically vigorous mixing is not required. The process can optionally include adding of a solid filter aid (e.g., polymer or spent bleaching clay) to the Decanter Centrifuge 406 stage with the water, which can help aid in solid removal in a subsequent removal step. The water/oil wash mixture may be fed inline to a horizontal type centrifuge decanter that is designed to remove solids or contaminants in the oil. Alternative decanting methods, such as basket filtration or other centrifugation processes, can be used. The decanting is intended to remove gums and solids 408 that are precipitated from the oil with the small addition of water.
The process 400 may feed the water treated mixed oil to Chemical Mixing stage(s) 412 where a chelate is added to the water treated oil mixture. The mixture is mixed vigorously through an inline dynamic high-shear mixer, and inline fed to a subsequent stage. Alternatively, other mixing methods such as flow-through restriction via an inline static mixer or aggressive agitation may be used. The chelate added may be sodium salts of EDTA that is added to the oil based on the level of calcium, magnesium and iron in the oil. The amount of EDTA added may typically be from 1-3 times the amount needed stoichiometrically based on remaining iron, calcium and magnesium. Additional water typically is added during this stage. Additionally, acids or bases may be added to the chelate/water mixture to assure ideal pH. Depending upon the metals being removed, pH of the water phase is typically within a range of 3.5-7. For optimal removal of NHP, particularly phosphatidic acid (PA), a pH higher than the pka of PA (approximately 2.6) is desired to assure the de-metaled PA is charged and migrates to the water phase.
The material is then fed to a pH adjustment Reactor 414, where the chelate/oil mixture is maintained for a period of time while continuing to be agitated and/or stirred to assure complete contact and to allow hydration to occur. This contact stage can last for a few minutes up to several hours. However, the chelate/oil mixture continues to be stirred, recirculated or otherwise agitated to avoid settling or separation and ensure continued contact and interaction between the surface area of microbubbles of water and the oil/chelate mixture formed during the mixing stage to cause the reaction to move the phosphorus out of the lipid containing phase and into the water phase. For example, the inline process may include optionally an additional shear mixer implementing a recycle loop to avoid settling and to keep the water droplets in the oil/acid mixture small and dispersed throughout the oil/acid mixture. In this pH adjustment stage 414 the acid treated oil mixture is fed to an inline stir tank and is mixed with the addition of an acidic or basic substance, to further adjust pH. The inline mixing during this pH adjustment stage is not vigorous like in the Chemical Mixing Stage(s) 412. Alternative processing may raise the pH to above neutral to remove free fatty acids (FFA) in feedstocks with FFA content below about 3%. Water may optionally be added to the mixture to allow a larger volume of liquid to remove contaminants in a subsequent stage (e.g., from 5-10% by volume of the oil). To avoid a significant amount of soapstock production, the optimal pH is well below the pka of the free fatty acids (FFAs). Likewise, to assure complete removal of hydrated gums, the pH is above the pKa of PA. Thus the pH is maintained from about 2.5 to 7 for optimal processing. Further, salts such as Sodium Sulfate and Sodium Chloride can be added in this stage to help reduce the stability of emulsions and improve downstream separation.
The adjusted pH oil mixture is fed to a centrifuge separator 416 (Centrifuge 1) in degumming to remove the water phase and gums 418 from the oil/water mixture. The separated waste water and gums 418 are sent to waste treatment.
The partially degummed oil is fed to a second Reactor 420 (Reactor 2) where the partially-degummed oil is optionally mixed with an additional chelating substance 422, such as a sodium salt of ethylenediaminetetraacetic acid (EDTA), to further hydrate phospholipids for removal. The amount of EDTA added may typically be from 1-3 times the amount needed stoichiometrically based on remaining iron, calcium and magnesium. The EDTA is an aqueous solution, which may have a total amount of water from 2-5% volume basis related to the oil. Other chelate substances may be used, including a wide range of polycarboxylic acids and polymers. Optionally, the solution of EDTA may be a different salt (e.g., potassium). The EDTA solution may optionally be pH adjusted with an organic acid such as citric acid. Since metals have different optimal pH levels for binding with chelates, the pH of this stage may be different than in the initial chelate binding stage. In some implementations, a salt, such as Sodium Chloride or Sodium Sulfate, may optionally be added to limit the formation of emulsions.
In a second Centrifugation state 424 (Centrifuge 2) the chelate-mixed oil is centrifuged to remove the water phase 426. The removed water may contain the majority of the remaining gums.
The lipid containing phase may be fed to a third reactor 428 (Reactor 3). Water, from 2-5% relative to the lipid containing phase, may be added to wash the lipid containing phase prior to being fed into the inline centrifuge separator in the third centrifuge stage 432 (Centrifuge 3) where the water phase 434 is removed. Additionally, further chemical additives 430 may be added in this stage, for example such as chelating materials. Acid and base may be used to pH adjust the aqueous phase.
The double-cleaned oil may be fed to a vacuum flashing vessel 436 and/or a drying reactor 438, where it is subject to inline dehydrating at vacuum to remove essentially all remaining water with a target of 0.1-0.3%. The pressure of the mixture may be reduced to around 500 millimeters of mercury on an absolute scale. The mixture may be heated to 200 to 210 degrees F. and held for 10 to 40 minutes. The vacuum can be achieved by a vacuum system 440, which generates a vacuum via a vacuum pump, steam ejector or similar process.
The dried oil may be fed to one or more Bleaching Reactors 442 following the vacuum drying, where the oil may be combined with an adsorbent material, for example such as bleaching clay ranging from 0.2% to 0.5% clay to the volume of oil. Other adsorbents such as silicas, activated carbon or finely powdered aluminas may also be used to address specially-required chemical actions including the removal of organic chlorides and sodium. Other materials, such as filter aids, may be added to ease later recovery. The oil may then be sent to Bleaching Filters 446, where the oil may be filtered through a deep-cake Neutsche-type filter, a pressurized leaf filter or other types of filters (e.g., pressurized candle filters) in order to remove the adsorbent and any adsorbed contaminants.
The filtration may be aided by a filter precoat system 448, which deposits a filter aid on the filtering elements, using materials such as polymers, diatomaceous earth or other filter aids. This helps assure that all adsorbent is recovered and removed from the lipid containing substances.
The purified oil may be stored, at product storage 452, until delivery to customers, at 454.
Some embodiments feature a two-stage degumming process. In these embodiments, the first degumming stage uses a chelate treatment. The first degumming stage may be followed by a second degumming stage using additional chelates. In some examples, the chelate is Ethylenediaminetetraacetic acid (EDTA).
This two-stage process may remove essentially all phosphorous (via phospholipids). Additionally, having two stages that are each able to remove a large amount of phospholipid provides a large amount of flexibility. Most edible oil facilities process one type of oil continuously. The disclosed technologies may process multiple types of oil. For example, a plant implemented process may handle animal fat one day, then corn oil the next and soy the following, and all are waste products with a lot more variability than an edible oil. These variabilities may include phospholipids, potassium, magnesium, sulfur, nitrogen, metals contamination levels, viscosity, and sediments in the feed oil. Each feed oil has different behavior, and in the event of an issue (e.g., the first stage forms emulsions and a lot of phospholipid gets carried over), there is the ability to complete degumming with the second stage.
The oil refining process 100 may process many different feedstock types. For example, the feedstock types may include crude soybean oil, crude degummed soy oil, canola oil, palm oil, used cooking oil, corn oil, distillers corn oil, sorghum oil, rapeseed oil, camelina, beef tallow, fish oil, algal oil, yellow grease, some blends of brown grease, white grease, poultry fat, hog fat, and similar feedstock types. The finished product from the oil refining process 100 may be a deep degummed and super-bleached renewable diesel plant feedstock.
Referring to
The degumming subprocesses 101, 102 may receive the crude feed LCC 106 as an input, and may degum the crude feed LCC 106 to produce degummed LCC 118 using water 108, acid 110, caustic 112, chelate 114, and similar inputs. Byproducts of the degumming subprocess 102 may include water, gums, and trace metals 116.
The acid degumming subprocess 101 may receive the crude feed LCC 106 as an input, and may degum the crude feed LCC 106 using water 108, acid 110, caustic 112, and similar inputs. For example, after treatment of the crude LCC with water 108 and acid 110, a caustic 112 may be used to partially neutralize the resulting acidic mixture. Centrifugation may be used to separate the water phase from the lipid containing phase. The water phase may then be removed.
The chelate degumming subprocess 102 may optionally receive the lipid containing phase produced by the acid degumming subprocess 101 as an input, and may degum the lipid containing phase using one or more chelates 114 to produce degummed LCC 118. In some embodiments, the chelates 114 may include EDTA.
The adsorptive bleaching/drying subprocess 104 may receive the degummed LCC 118 as an input, and may process the degummed LCC 118 to produce purified LCC 126 using bleaching clay 120 and similar inputs. Byproducts of the adsorptive bleaching/drying subprocess 104 may include spent clay and trace contaminants 122 and water 124.
The process 100 may include additional steps, for example including decanting, additional centrifugation, vacuum drying, filtering with bleached earth, and the like.
The process 200 may include a heat subprocess 202. During this subprocess, the feed LCC 232 is heated to a processing temperature. The processing temperature may be 140-190 F. The heating may be implemented using a batch heating in tank or through an inline heat exchanger.
The process 200 may include a first mix subprocess 204. During this subprocess, water 234 may be added to the heated feed LCC. The water 234 may be deionized water. The added water 234 may be 1-2% by volume. The mixing may be implemented by an inline static mixer to ensure water distribution throughout the LCC. This mixing need be only vigorous enough to assure contact of the feed LCC and water. For example, this mixing may be implemented using a stirred tank or similar mixer. A solid filter aid may be added here for solid removal. For example, the solid filter aid may be polymer or a spent adsorbent such as bleaching clay.
The process 200 may include a decant subprocess 206. Here the water/LCC mixture may be fed to a decanter. The decanter may be a horizontal-type centrifuge designed to remove waste solids or contaminants 236 from the LCC. For example, the horizontal-type centrifuge may operate at a relatively low speed of ˜2500-4000 RPM, and may be a machine in the 100-200 horsepower range. Alternatively, methods such as basket filtration or other centrifugation processes may be used here. This subprocess 206 may remove solids that are easily formed with a small addition of water. A countercurrent scroll may operate within the centrifuge's bowl to push solids to a discharge port. The cleaned LCC may proceed to a clean LCC discharge port. In some embodiments, a small addition of water may be used to help remove remaining hydratable phosphatide gums.
The process 200 may include a second mix subprocess 208. Here an acid 238 may be added to the mixture. For example, phosphoric acid may be added to the LCC mixture according to the level of phosphorus in the mixture. Alternatively, other acids may be used. For example, citric, oxalic, tartaric, or other organic acids with some chelating ability may be added. For most LCCs 0.3% concentrated acid will suffice. Additional water may be added. The total concentration of acid in water, including water 234 added during mix subprocess 204, may vary from 10-15%. Depending upon the LCC being treated, acidity of the water phase may fall within a range of 1-3.5 pH.
In this subprocess 208, the mixture may be mixed vigorously. For example, an inline dynamic high-shear mixer may be employed for the mixing. Alternatively, other mixing methods may be used. For example, flow-through restriction via an inline static mixer or aggressive agitation may be employed for the mixing.
The process 200 may include a hold subprocess 210. In this subprocess, the acid/oil mixture may be held for a hold interval to assure complete contact, and to allow hydration to occur. The duration of this hold interval may range between a few minutes and several hours. An additional shear mixer may be added here on a recycle loop, for example to keep the water droplets in the oil/acid mixture small. In some embodiments, the pH of the mixture may be reduced below the pKa of phosphaditic acid (PA). For example, the pH of the mixture may be reduced to lower than 2. This process breaks apart the PA-Ca or PA-Mg complexes that are oil soluble.
The process 200 may include a pH adjustment subprocess 212. In this subprocess, the mixture is partially neutralized with a base 240. For example, the base may be sodium hydroxide, ammonium hydroxide, potassium hydroxide, or similar alkali substances. The pH adjustment may bring the pH of the water phase to a range from 4-7. Alternatively, the mixing may raise the pH of the mixture above neutral, for example to remove free fatty acids in feedstocks with a free fatty acid (FFA) content below about 3%. Water 242 may be added to the mixture to allow a larger volume of liquid to remove contaminants. For example, the added water may range from 5-10% by volume of the oil mixture. The water 242 may be deionized water. The mixing in this subprocess need be only vigorous enough to assure contact between the base and the mixture. For example, this mixing may be implemented using a stirred tank or similar mixer. In some embodiments, the pH of the mixture may be increased above the pKa of phosphaditic acid (PA), but below that of full neutralization. The pH of the mixture may be increased to the range of 2.5 to 7. The pH of the mixture may be increased to the range of 4 to 6. This partial neutralization ensures a majority of free fatty acid in the mixture is not converted into soapstock. In contrast, current approaches employ full neutralization, taking the pH of the mixture well above 7. Such approaches are not useful with feedstocks having high levels of free fatty acids because free fatty acids would be present in the finished product at high levels.
The process 200 may include a first centrifuge subprocess 214. Here, the mixture is centrifuged and the water phase 244 is removed. The removed water phase 244 may be sent to waste treatment.
The process 200 may include a second centrifuge subprocess 216. Here, the cleaned oil may be washed with water 246 and centrifuged to further remove contaminants. For example, the added water may range from 2-10% by volume of the oil mixture. The water 246 may be deionized water.
The process 200 may include a third mix subprocess 218. Here, the partially degummed oil is optionally mixed with a chelate 252 to further hydrate phospholipids for removal. For example, the chelate 252 may be a sodium salt of EDTA, potassium, or similar salts. Vigorous mixing is not required. Only light mixing is needed. The solution may be pH-adjusted with an organic acid, for example such as citric acid.
A salt such as sodium chloride or sodium sulfate may be added, for example to limit formation of emulsions. Alternatively, other chelates known to someone skilled in the art may be used, for example including a wide range of polycarboxylic acids and polymers containing such acids. The amount of chelate 252 added may range from 1-3 times the amount needed stoichiometrically based on remaining iron, calcium, and magnesium. Water 250 may be added as well. For example, the added water may range from 2-5% by volume of the oil mixture. The water 246 may be deionized water.
The process 200 may include a third centrifuge subprocess 220. Here, the mixture may be centrifuged to remove the water layer 254, which may contain the majority of the remaining gums. The lipid containing phase may be retained.
The process 200 may include a fourth centrifuge subprocess 222. Here, the lipid containing phase may washed with water 256, from 2-5% by volume, and centrifuged again to remove water and contaminants 258. The water 256 may be deionized water.
The process 200 may include a vacuum dry subprocess 224. Here, the cleaned oil may be dehydrated at vacuum to remove water 260. For example, water remaining in the mixture after this subprocess may be approximately 0.1%.
The process 200 may include a bleach subprocess 226. Here, the oil may be combined with an adsorbent 262. The adsorbent may be bleaching clay. The added adsorbent may range from 0.4 to 0.6% of the oil by weight. Other materials, such as filter aids, may be added to ease later recovery.
The process 200 may include a filter subprocess 228. Here, the clay/oil mixture may filtered to remove the spent adsorbent 264 and any adsorbed contaminants. The filter may be a deep cake Neutsche type filter, a pressurized leaf filter, a pressurized candle filters, or other type of filter. The result is purified LCC 266. In some embodiments, this purified LCC 266 may have a free fatty acid content above 2%. In some embodiments, this purified LCC 266 may have a phosphorus content below 3 ppm.
The process 500 may include a heat subprocess 502. During this subprocess, the feed LCC 532 is heated to a processing temperature. The processing temperature may be 140-190 F. The heating may be implemented using a batch heating in tank or through an inline heat exchanger.
The process 500 may include a first mix subprocess 504. During this subprocess, water 534 may be added to the heated feed LCC. The water 534 may be deionized water. The added water 534 may be 1-2% by volume. The mixing may be implemented by an inline static mixer to ensure water distribution throughout the LCC. This mixing need be only vigorous enough to assure contact of the feed LCC and water. For example, this mixing may be implemented using a stirred tank or similar mixer. A solid filter aid may be added here for solid removal. For example, the solid filter aid may be polymer or a spent adsorbent such as bleaching clay.
The process 500 may include a decant subprocess 506. Here the water/LCC mixture may be fed to a decanter. The decanter may be a horizontal-type centrifuge designed to remove waste solids or contaminants 536 from the LCC. For example, the horizontal-type centrifuge may operate at a relatively low speed of ˜2500-4000 RPM, and may be a machine in the 100-200 horsepower range. Alternatively, methods such as basket filtration or other centrifugation processes may be used here. This subprocess 506 may remove solids that are easily formed with a small addition of water. A countercurrent scroll may operate within the centrifuge's bowl to push solids to a discharge port. The cleaned LCC may proceed to a clean LCC discharge port. In some embodiments, a small addition of water may be used to help remove remaining hydratable phosphatide gums.
The process 500 may include a second mix subprocess 508. Here a chelate 538 may be added to the mixture. For example, EDTA may be added to the LCC mixture according to the level of calcium, magnesium and Iron in the mixture. Alternatively, other chelates may be used. Additional water may be added. Depending upon the LCC being treated, pH of the water phase may fall within a pH range of 3.5-7
In this subprocess 508, the mixture may be mixed vigorously. For example, an inline dynamic high-shear mixer may be employed for the mixing. Alternatively, other mixing methods may be used. For example, flow-through restriction via an inline static mixer or aggressive agitation may be employed for the mixing.
The process 500 may include a hold subprocess 510. In this subprocess, the chelate/oil mixture may be held for a hold interval to assure complete contact, and to allow hydration to occur. The duration of this hold interval may range between a few minutes and several hours. An additional shear mixer may be added here on a recycle loop, for example to keep the water droplets in the oil/chelate mixture small.
The process 500 may include a pH adjustment subprocess 512. In this subprocess, the mixture is partially neutralized with an acid or base 540. For example, the base may be sodium hydroxide, ammonium hydroxide, potassium hydroxide, or similar alkali substances. The neutralizing may bring the pH of the water phase to a range from 3.5-7. Alternatively, the mixing may raise the pH of the mixture above neutral, for example to remove free fatty acids in feedstocks with a free fatty acid (FFA) content below about 3%. Water 542 may be added to the mixture to allow a larger volume of liquid to remove contaminants. For example, the added water may range from 5-10% by volume of the oil mixture. The water 542 may be deionized water. The mixing in this subprocess need be only vigorous enough to assure contact between the acid or base and the mixture. This partial neutralization ensures a majority of free fatty acid in the mixture is not converted into soapstock. Additionally, salts such as Sodium Chloride and Sodium Sulfate may be added at this stage to help break emulsions formed in the shear mixing subprocess.
The process 500 may include a first centrifuge subprocess 514. Here, the mixture is centrifuged and the water phase 544 is removed. The removed water phase 544 may be sent to waste treatment.
The process 500 may include a second centrifuge subprocess 516. Here, the cleaned oil may be washed with water 546 and centrifuged to further remove contaminants. For example, the added water may range from 2-10% by volume of the oil mixture. The water 246 may be deionized water.
The process 500 may include a third mix subprocess 518. Here, the partially degummed oil may be mixed with additional chelate 552 to further hydrate phospholipids for removal. For example, the chelate 552 may be a sodium salt of EDTA, potassium, or similar salts. Vigorous mixing is not required. Only light mixing is needed. The solution may be pH-adjusted with an organic acid, for example such as citric acid. The pH of this stage may be different than the pH of the pH adjustment stage, since binding affinity of chelates to metals is optimal at different pH for different metals. This stages pH may be adjusted based on residual metals present after the first stage. In some embodiments, the pH of this stage may be approximately neutral, while the pH of the pH adjustment stage may be approximately the same as the pKa of phosphaditic acid. In some embodiments, the pH of this stage may be the same as the pka of phosphaditic acid, while the pH of the pH adjustment stage may be approximately neutral. In some embodiments, the pH of this stage may be 5-7, while the pH of the pH adjustment stage may be 3-4. In some embodiments, the pH of this stage may be 3-4, while the pH of the pH adjustment stage may be 5-7.
A salt such as sodium chloride or sodium sulfate may be added, for example to limit formation of emulsions. Alternatively, other chelates known to someone skilled in the art may be used, for example including a wide range of polycarboxylic acids. The amount of chelate 552 added may range from 1-3 times the amount needed stoichiometrically based on remaining iron, calcium, and magnesium. Water 550 may be added as well. For example, the added water may range from 2-5% by volume of the oil mixture. The water 546 may be deionized water.
The process 500 may include a third centrifuge subprocess 520. Here, the mixture may be centrifuged to remove the water layer 554, which may contain the majority of the remaining gums. The lipid containing phase may be retained.
The process 500 may include a fourth centrifuge subprocess 522. Here, the lipid containing phase may washed with water 556, from 2-5% by volume, and centrifuged again to remove water and contaminants 558. The water 556 may be deionized water.
The process 500 may include a vacuum dry subprocess 524. Here, the cleaned oil may be dehydrated at vacuum to remove water 560. For example, water remaining in the mixture after this subprocess may be approximately 0.1%.
The process 500 may include a bleach subprocess 526. Here, the oil may be combined with an adsorbent 562. The adsorbent may be bleaching clay. The added adsorbent may range from 0.4 to 0.6% of the oil by weight. Other materials, such as filter aids, may be added to ease later recovery.
The process 500 may include a filter subprocess 528. Here, the clay/oil mixture may filtered to remove the spent adsorbent 564 and any adsorbed contaminants. The filter may be a deep cake Neutsche type filter, a pressurized leaf filter, a pressurized candle filters, or other type of filter. The result is purified LCC 566. In some embodiments, this purified LCC 566 may have a free fatty acid content above 2%. In some embodiments, this purified LCC 566 may have a phosphorus content below 3 ppm.
The present application claims priority to U.S. Provisional Patent Application No. 63/469,795, filed May 30, 2023, entitled “PROCESSING LIPID-CONTAINING COMPOUNDS FOR FUEL FEEDSTOCK THROUGH MULTISTAGE DEGUMMING AND ADSORPTIVE BLEACHING/DRYING,” the disclosure thereof incorporated by reference herein in its entirety.
| Number | Date | Country | |
|---|---|---|---|
| 63469795 | May 2023 | US |
