• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
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  • 引用文献
  • 法律状态
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    • 专利摘要:
    The present invention relates to a process of regeneration of used lubricating oils consisting of a triple distillation process including a second column of deasphalting and activation of caustic reagent. The invention is basically characterized by the independent deasphalting phase, which is described in the figure. This deasphalting is done in an independent column, obtaining an asphaltic bottom without additive, since the additivation of the caustic reagent is also carried out in the deasphalting column, but in a phase immediately after the extraction of the asphaltic bottom. The process allows to obtain high quality lubricant bases using low concentrations of caustic reagent and produces an asphaltic bottom in the second column of high quality, because it does not contain caustic reagent. In this way, the production of waste is also significantly reduced. (Machine-translation by Google Translate, not legally binding)
    公开号:ES2629851A1
    申请号:ES201600114
    申请日:2016-02-15
    公开日:2017-08-16
    发明作者:José Antonio GÓMEZ MIÑANA
    申请人:José Antonio GÓMEZ MIÑANA；
    IPC主号:
    专利说明:

    Triple distillation procedure for the regeneration of used oils including caustic treatment in line in the second distillation. Technical sector
    The present invention relates to the regeneration sector of used mineral oils, an industrial operation that consists in recovering, from used lubricating oils, from the automotive industry and industry, that they have lost their initial properties and which are highly contaminating lubricant bases They can be reused again.
    Specifically, the invention relates to a process that significantly improves the currently existing procedures, increasing the quantity and quality of reusable products and significantly reducing the volume of waste generated. Background of the invention
    Mineral oils used due to their volume and dispersion, are one of the most important industrial waste and with the greatest polluting potential. Therefore, historically, many methods of managing them have been developed.
    Unlike recovery, which involves a lower step in the hierarchy of waste, regeneration, which in some countries is called re-refining, is a recycling process in which lubricant bases are obtained similar to those of the first refining of the oil, that is, it is a process of recycling material back to the original product.
    The first processes of regeneration or re-refining of the used lubricating oils appeared in the 1960s and were well received because they contributed to reduce the contamination of soils and waters where until that moment, part of those used oils were going to stop while another an important part was burned as alternative fuels in an uncontrolled way, which transferred the pollution they contained to the atmosphere.
    In Spain, a pioneer country in this field, the collection and regeneration of used oils began in the 1960s. The processes developed in Spain produced good quality bases, compared to other processes in other countries, but suffered from the same defect of generate highly polluting waste, because chemical reagents (sulfuric acid) were used that gave rise to acid residues that are difficult to remove. Plants with these processes are still in operation in many developing countries.
    Over the years, regeneration techniques were necessarily changing, among other reasons because the characteristics of used oils were also changing. In lubricating oils, the proportion of additives that appeared in its formulation was significantly increased, in response to the greater demands of the engines where they were used, which resulted in the processes used until then ceasing to be operational.
    Of all the processes that are currently used, one of the most advanced is a process that was once patented by the Italian company Viscolube with international publication number WO 94/07798, of which the author of the present patent application is co-author .
    The indicated process consists of:
    1) Addition to the used oil of an alkaline reagent.
    2) Thermal dehydration of used oil and subsequent water and light condensation. (Preflash)
    3) Deasphalting-demetallizing-fractionation by vacuum distillation that results in the separation of an asphalt bottom that contains all the oxidation and contamination products that the used oil contains, the additives of the degraded lubricant and the reagents added in the process itself. At the same time the distillates are separated into several lubricant fractions of increasing viscosities.
    4) Discoloration treatment of distilled fractions with bleaching earth to obtain regenerated lubricant bases.
    This process has been for many years one of the most suitable for regeneration plants of relatively small dimensions (Up to 50,000 t / year of treatment) and, both the yields and the qualities of the products obtained, were the best among all the processes then used to obtain bases of Group I, according to the API classification (American Petroleum Institute) Viscolube subsequently modified the process by replacing the treatment with bleaching earth with a hydrogenation treatment, thus obtaining lubricant bases of the Group II API. However, changes in the composition of the raw material (used oil) have been causing problems in the treatment, leading to an increase in the cost of processing and a decrease in the quality and yields of the products obtained. This variation in the composition of the used oils also causes fouling problems inside the deasphalting column.
    One of the main causes of the variation of the characteristics of the used oils is the use in the lubricants of origin of, every time greater amount of synthetic fluids type esters that, when mixed in the collection with the mineral oils, cause serious treatment problems
    For this reason, some processes that were optimal a few years ago have come to present difficulties in the treatment resulting in a lower yield, greater reagent consumption and in some cases the impossibility of treating certain used oils due to their high proportion in contaminants.
    Another process scheme widely used in the regeneration of used oils is the processes that use solvent extraction systems. These processes are also used in many facilities worldwide, although they are remarkably different processes from the present patent application. Explanation of the invention.
    The object of the invention consists in a process of regeneration of used mineral oils, in which the steps of deasphalting and addition of alkaline reagent are carried out in an independent column designed especially and exclusively for these functions. In this way, the deasphalting phase is independent of the fractionation phase, while the addition of the alkaline reagent goes from being at the head of the process to this unit. This column is placed immediately after a conventional dehydration column.
    Deasphalting and the addition of alkaline reagent occurs, within the column, in two successive phases, so that the effectiveness of the alkaline treatment is increased by having been carried out after the elimination of most of the contaminants with which it could react. In this way, greater efficiency in the activity of the reagent is achieved, very significantly reducing the amount of reagent and improving the quality of the final products obtained.
    On the other hand, the fact that the reagent is added after the extraction of the deasphalting products by the bottom of this column, has the consequence that both the alkaline reagent and its compounds are absent in the composition of this background of reaction, which converts this product of desasfaltado in a usable product of greater quality, avoiding that it must be managed, in many cases, as a by-product of low quality, or as a waste.
    Then, the fraction distilled together with the reagent is taken to the third distillation column, where the contaminating metals that have still been dragged along with the reagent are separated from the bottom and, laterally, a series of lubricating fractions that Its high quality can be used without further treatment as bases for the manufacture of commercial lubricants.
    Consequently, the advantages obtained with the use of the claimed process are the following:
    1) The asphalt fraction that is extracted from the bottom of the deasphalting column does not contain traces of the alkaline reagent or the metals or compounds that react with this product. Therefore, an asphalt fraction of much higher quality is obtained that allows its use in application is not achievable with that obtained with existing systems.
    2) Eliminating the asphalt fraction before incorporation of the alkaline reagent allows it to react much better, since a large part of the compounds that were in the bottom of the distillation and that reacted with this reagent without any benefit have been removed and with a higher consumption of it. This results in the reagent consumption being remarkably lower and the quality of the products obtained much higher.
    3) As indicated, in the used oils that are used as raw material, ester type synthetic compounds appear in increasing proportion. These compounds are largely derived from the emptying of hydraulic systems. When these esters react with the alkaline reagent they result in the production of soaps that hinder or even prohibit the treatment of certain used oils. As in the case of this invention, the alkaline reagent is added after the deasphalting stage, and, since a large part of these esters have been eliminated as the background of this distillation, the problem disappears or is greatly attenuated, which allows treating used oils that otherwise they would not be regenerable.
    4) The high quality of the fractions obtained makes unnecessary, or drastically decreases, the consumption of bleaching earth for the finishing of the fractions resulting in a drastic decrease in the amount of waste and, consequently, in the cost of its elimination. Brief description of the drawings
    Two schemes are illustrated that illustrate the possibility of realization and application of the invention:
    Figure 1 describes the stages of the complete regeneration process complete, with the three distillation columns: Dehydration, deasphalting and fractionation. Additionally, as indicated in Figure 1, a hydrogenation phase can optionally be included in order to achieve Group II API oils.
    Figure 2 describes in detail the thermal deasphalting phase, including the column and the reagent additive, from the entry of the dehydrated product to the shipment to the fractionation column. Application of the invention
    An operation scheme of a used oil regeneration plant with three distillation columns, as shown in the present invention, is shown in Figure 1. The phases indicated are the following:
    - Dehydration: At this stage, which is common in many of the regeneration processes, water and light hydrocarbons that are present in the used oil are eliminated. As much water as light hydrocarbons are removed by evaporation in a distillation column, which normally works at low temperature and moderate vacuum. Water and evaporated solvents condense and reach a decanter where they separate. Water is treated for recovery or is disposed of as waste. The hydrocarbons are processed for later use.
    - Deasphalting and additive reagent: In this phase three products are obtained: Asphalt-type components at the bottom of the column, stream of diesel-type light fraction at the top of the column and cutting of lubricating fractions at the center of the column. The distillation is carried out under high vacuum (10 mbar) and the separation of an asphalt product that does not contain metals from the caustic reagent or the reaction products with said reagent is achieved. This results in obtaining a product suitable for use as an asphalt additive in the preparation of blown asphalts and as a component of asphalt waterproofing fabrics. The column is designed to achieve a good separation of these asphalt components that do not distill, from the rest of the lighter hydrocarbons that are extracted from the top while a lateral extraction is obtained the cut that comprises all the lubricating fractions. During the deasphalting process, the caustic reagent that reacts with the undesirable compounds that distill at the same temperature as the cutting of the lubricant fractions is added. The addition of the in-line reagent has been done to facilitate the reactive-oil reaction and at the same time avoid the sudden vaporization of the water that accompanies the reagent. This phase is explained in more detail in Figure 2.
    - Demetalized-Fractionation: Fractional distillation at high vacuum of the additive product (Third distillation), obtaining a minimum residual bottom current and three types of cutting of high quality lubricating bases. The design and operation of this third distillation column allows the elimination of a semi-solid residue from the bottom of the column and the obtaining of the lubricant bases by the lateral extractions. However, the residual column bottom represents a much smaller volume than in other technologies due to the existence in the process of an independent deasphalting phase.
    - High Pressure Hydrogenation Treatment: This stage is optional and only if you want to obtain bases of Group II API. However, this invention significantly reduces the consumption of catalysts and hydrogen in the hydrogenation phase with respect to processes with two distillations.
    Figure 2 represents in detail the phase of deasphalting and additive caustic reagent, as described below:
    - The oil that comes from the dehydration phase is previously stored in a feed tank (1). This tank is provided with insulation to prevent oil cooling and, in order to homogenize it and maintain its temperature at 120 ° C, there is a recirculation equipment provided with a pump (2) and a heater (3).
    - Subsequently, with a high pressure pump (4), the oil is sent to the oven (5). The oil temperature rises to 360 ° C and, through the transfer line reaches the column (6). A vacuum equipment allows the Flash Zone of this column to be at an absolute pressure of 10 mm of mercury. Under these conditions of pressure temperature a separation of all those compounds that do not distill which are extracted by the bottom of the column by means of the pump (7) is carried out.
    - The bottom fraction is mainly composed of high distillation hydrocarbons, additives present in the initial lubricating oil that were incorporated to improve its characteristics (detergents, antioxidants, etc.) as well as viscosity index improver additives used in Multigrade oils. Other contaminants such as dust, coal, etc. are also present. that contaminate the used oil and make its change necessary. This bottom distillation fraction can be used in various uses, such as component in the manufacture of waterproofing for asphalt fabrics, and similar applications. It can also be used as fuel in facilities where your equipment allows it.
    - The volatile fraction in the conditions of the Flash Zone passes to the immediately upper part of the column and there is a falling stream of cold liquid that produces partial condensation of it.
    - The condensed fraction is extracted with the pump (8). This pump sends the oil to the refrigerant (9) and a part of it is sent back to the column (6). In a level controller located in the column, it sends the excess product (demetallized oil) to the intermediate storage tank (10).
    - A certain amount of Reagent solution, which is mixed and homogenized in the mixer (12), is incorporated into the stream that is recirculated to the column. With the incorporation of this reagent, the characteristics of the distilled fractions are greatly improved.
    - The column is specifically designed to prevent fouling due to the caustic additive and the reaction compounds of this reagent with the components present in the distillates with which this reagent acts.
    - Therefore, instead of filling or plates, it has been designed with inclined baffles, these baffles are perforated to improve the vapor / liquid exchange, as well as to reduce the fouling thereof.
    - The non-condensing part of the rising vapors passes to the top of the column, where it meets another cold descending stream. This cold current comes from the recirculation of the liquid through the pump (13) that passes the current through the Refrigerant (14).
    - Excess product, indicated by a level controller, is taken to the diesel storage tank.
    - Water vapor that does not condense under the conditions maintained at the top of the column and some incondensable hydrocarbons reach the condenser (15). This condenser is fed with coolant (Brine) at 2 ° C to condense most of the water and light hydrocarbons, thus achieving a better vacuum and a decrease in the size of the vacuum equipment.
    - The uncondensed vapors arrive at the vacuum equipment (16) which is composed of a Liquid Ring Pump and two Boosters. All condensates, as well as the non-condensable vapors, are returned to the decanter (17) of the dehydration phase for separation and treatment.
    - Therefore, in the phase of desasfaltado the following fractions are obtained:
    1) Water and light hydrocarbons: In the head condensers.
    2) Diesel: At the top of the column.
    3) Demetalized oils: In the central part of the column.
    4) Background Fraction: At the bottom of the column.
    权利要求:
    Claims (4)
    [1]
    1. New procedure for the regeneration of mineral oils used with triple
    distillation consisting of a dehydration column, a deasphalting column 5 and a fractionation column.
    [2]
    2. The method according to the preceding claim wherein the deasphalting column includes a process for the additive of caustic reagent after the extraction of the contaminating compounds present in the used oil.
    [3]
    3. Method according to the preceding claims in which the additive of the caustic reagent occurs at low concentrations, less than 3%.
    [4]
    4. Process according to the preceding claims, wherein the distilled fractions 15 are treated with hydrogen.
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    同族专利:
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    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    ES476872A1|1978-01-12|1979-06-01|Snam Progetti|Process for regenerating exhausted oils|
    EP0574272A2|1992-06-12|1993-12-15|Chemical Engineering Partners|Improved process for the production of base stock oils from used oil|
    ES2222051T3|1998-11-11|2005-01-16|Mineralol-Raffinerie Dollbergen Gmbh|RECOVERY PROCEDURE OF USED OILS.|
    WO2010050901A1|2008-10-31|2010-05-06|Annda Energy Pte Ltd.|Process and system for recovering base oil from lubrication oil that contains contaminants therein|
    WO2015067828A1|2013-11-08|2015-05-14|Sener Ingenieria Y Sistemas, S.A.|Method for increasing the yield of lubricating bases in the regeneration of used oils|
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