CN113101699B - Self-extraction purification process for residue-containing dirty oil - Google Patents
Self-extraction purification process for residue-containing dirty oil Download PDFInfo
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Abstract
The invention provides a self-extraction purification process of dirty oil containing slag, which comprises the steps of continuously pretreating, extracting and evaporating the dirty oil containing slag under a closed condition; the method specifically comprises the following steps: removing part of mechanical impurities from the dirty oil containing the residues through pretreatment; adding light oil and water into the dirty oil with part of mechanical impurities removed for extraction treatment to obtain sewage and extracted dirty oil; evaporating the extracted dirty oil to obtain light oil, water and purified oil; and recycling the light oil and the water obtained by evaporation for the extraction treatment. The purification process provided by the invention is suitable for treating refinery sump oil, is low in cost, hardly generates waste gas and waste residue to pollute the environment, and can realize maximum resource recovery.
Description
Technical Field
The invention belongs to the technical field of treatment of residue-containing dirty oil generated in production processes of refineries or oil extraction and the like, and particularly relates to a process for cleaning the residue-containing dirty oil.
Background
With the rapid development of modern society and economy, the dependence of human society on energy is increasing, and it is well known that petroleum occupies the most important position in energy. With the rapid development of petrochemical industry, environmental problems caused by production are more and more serious, and the problems of effective utilization of resources and environmental protection are more and more concerned by people and become the focus of the current society. In recent years, new laws and regulations such as environmental protection law, ten items of gas, ten items of water, ten items of soil, new standards for pollution emission in petroleum refining industry and petrochemical industry are intensively developed in China, environmental protection policy leads to the change from total pollutant control to environmental quality improvement, higher requirements are put on environmental protection work of refining enterprises, and environmental protection situations of the refining enterprises are very severe.
The existing large amount of slag-containing dirty oil in the refining industry mainly comes from an electric desalting emulsion layer of an atmospheric and vacuum distillation unit, floating oil in an oil separation tank for sewage treatment, tank bottom cleaning dirty oil and the like, and the dirty oil occupies a storage tank for centralized storage, and if the dirty oil cannot be treated in time, the efficient operation of energy storage of a refinery is seriously influenced. At present, the treatment of the oil stain containing slag in a refinery mostly adopts a mode of field treatment by outsourcing for oil stain treatment enterprises. The treatment equipment is skid-mounted equipment, and the main process comprises the following steps: gravity settling method, heating settling method, hot water washing method, chemical demulsification dehydration method, electromagnetic field demulsification dehydration method, etc. The prior dirty oil purification treatment can generate a large amount of solid slag. The solid slag generates a large amount of VOCs in the drying process to form secondary pollution, and the solid slag is listed in national hazardous waste record, no. 251-001-08, and the treatment of hazardous waste causes new burden for the refining and chemical enterprises.
In conclusion, the conventional treatment method of crude oil containing slag does not meet the requirements of refining enterprises on safety and environmental protection.
The problem that how to purify and recycle the dirty oil containing the slag is troubling each refinery is the problem. Through literature and laboratory research, the difficulty of purifying the dirty oil is found as follows:
1. an oil displacement agent is added in the process of oil exploitation, the common oil displacement agent is a high molecular polymer, is a surfactant and is oleophilic and hydrophilic, and the formed emulsion is difficult to break emulsion and separate.
2. The oil product storage tank is injected with water and cleaning agent in the mechanical cleaning process, a large amount of charges are generated, the emulsification of oil, solid and water is intensified, and water-in-oil, oil-in-water, overlapping coating and other complex emulsions are formed.
3. The colloid, asphaltene, solid particles (such as clay fine powder, silicate and metal corrosion substances) dispersed in the crude oil can form stable emulsion, and are factors influencing difficult purification of the residue-containing dirty oil.
4. The residue-containing dirty oil accumulated at the bottom of oil production plants and crude oil tanks has extremely high salt content in emulsified oil, and has extremely high heavy metal content in the emulsified oil, which can aggravate the corrosion of processing equipment and the poisoning and inactivation of catalyst, and the treatment of desalting and demetalization is needed.
5. The emulsion dirty oil with different sources and properties is mixed and then is stored in a centralized way, so that the dirty oil has high water content and complex components, light residue enrichment can occur in centrifugal demulsification, an emulsion with high stability and difficult treatment is formed, and the resource recycling difficulty is high.
In the prior art, patent document CN 111234865A discloses a method for treating dirty oil, which realizes the treatment of dirty oil by at least six-stage filtration, and can obtain purified oil, sewage and solid slag which can be used for downstream equipment; patent document CN 109652119A discloses a dirty oil/aged oil treatment apparatus, which separates three phases of oil, water and solid in dirty oil by units of filtration, nucleation, centrifugation and the like. Patent document CN105694961a discloses a refinery effluent oil treatment system, which comprises an effluent oil pretreatment system, a three-phase separation system, a flocculant preparation system and a backwashing system, wherein the system obtains purified oil, sewage and solid residues by matching a three-phase separator with a flocculant. In the prior art, oil, water and slag in the residue-containing dirty oil are separated by filtration or centrifugation, the whole process cannot be closed in the purification process, a large amount of VOCS (volatile organic Compounds) can be generated, and air pollution is caused; the risk of blockage of the centrifugal and filtering equipment is increased along with the accumulation of the treatment capacity, the sudden shutdown of the equipment is usually accompanied by the occurrence of safety and environmental accidents, and the shutdown treatment also influences the production progress; in addition, the traditional dirty oil treatment method has a large amount of solid residues, and the demulsification separation is not thorough, so that the solid residues contain a large amount of oil, a large amount of solid residues are additionally treated for hazardous waste, and the resource is seriously wasted.
The inventor finds that solid residues generated by the prior sump oil technology are mostly macromolecular organic matters with serious emulsification except inorganic solids such as trace silt, rust and the like, and the macromolecular organic matters are derived from oil displacement agents, cleaning agents, colloids in crude oil, asphaltine and the like through laboratory research. After treatment by a suitable method, the so-called solid residues can be completely recycled into the oil and have no influence on downstream equipment.
In summary, by searching academic journals and patent technologies of dirty oil purification technology and understanding the existing dirty oil purification technology, the purification of dirty oil in petroleum refining enterprises and oil extraction enterprises adopts a filtration or centrifugation method. Due to the limitation of the process, the traditional sump oil purification cannot be completely closed, and VOCs are inevitably generated. In addition, the traditional centrifugal process can generate a large amount of solid slag, and for centrifugal rotating equipment, along with the accumulation of treatment capacity, the risk of equipment blockage and damage is gradually increased, so that unintended shutdown can be caused, and safety and environmental protection accidents can be caused in serious cases. Moreover, the mineral oil-containing solid slag is listed in the national hazardous waste record (No. 251-001-08), the state has strict regulations on hazardous waste treatment, and the solid slag generated by purifying the dirty oil is treated as the hazardous waste to cause the economic burden of secondary treatment for enterprises, but researches show that the solid slag mainly contains oil-soluble organic matters and is seriously wasted as the hazardous waste treatment. The existing dirty oil treatment technology cannot meet the green, safe and environment-friendly concept of high-quality development requirements, and the field operation environment cannot meet the requirements of new safe and environment-friendly regulations.
Therefore, it is necessary to provide a clean process for treating dirty oil in a refinery, which is simple in operation, low in cost, and capable of hardly generating waste gas and waste residue to pollute the environment and maximally recycling resources.
Disclosure of Invention
The purification process aims at the residue-containing dirty oil which is the dirty oil of an electric desalting emulsion layer of an atmospheric and vacuum distillation unit, the floating oil of a sewage treatment oil separation tank or the tank cleaning dirty oil at the bottom of various oil tank; the oil-displacing agent contains crude oil components and water, as well as water-soluble impurities such as metal ions and corrosive anions, inorganic impurities such as clay, silicate and metal corrosives, and organic impurities such as asphaltene, high-molecular oil-displacing agent and silicone oil.
The invention aims to: the purification process for the residue-containing waste oil is suitable for treating the waste oil in a refinery, low in cost, hardly generates waste gas and waste residue to pollute the environment, and can realize maximum resource recovery.
The above object of the present invention is achieved by the following scheme:
the self-extraction purification process of the residue-containing dirty oil comprises the steps of continuously pretreating, extracting and evaporating the residue-containing dirty oil under a closed condition; the method specifically comprises the following steps: removing part of mechanical impurities from the dirty oil containing the residues through pretreatment; adding light oil and water into the dirty oil with part of mechanical impurities removed for extraction treatment to obtain sewage and extracted dirty oil; evaporating the extracted dirty oil to obtain light oil, water and purified oil; and recycling the light oil and the water obtained by evaporation for the extraction treatment.
In the scheme of the invention, the light oil and the water used in the extraction treatment can be input from the outside of the system at the initial stage of the process, and in the subsequent continuous treatment, the light oil and the water come from the evaporation link of the process, so that the energy consumption can be saved, and the repeated processing of the oil for extraction can be avoided.
In the scheme of the invention, the light oil added at the initial stage of the process can be selected from various light petroleum products, such as naphtha, solvent oil, benzene, toluene, diesel oil and the like; preferably, one or a mixture of more than two of naphtha, solvent oil, benzene or toluene is used as an extracting agent; more preferably naphtha, 120# solvent oil, benzene, toluene, or a mixture of two or more thereof.
In a preferable scheme of the invention, the proportion of the light oil added into the dirty oil is 0.5 to 1.5 in terms of the weight ratio of the light oil to the dirty oil; more preferably 0.5 to 1.
In the scheme of the invention, the water added into the dirty oil with part of mechanical impurities removed can be water washing water, and the amount of the added water is 1 to 4 according to the weight ratio of the water to the dirty oil; more preferably 1 to 2.
In the scheme of the invention, the pretreatment can realize the removal of partial mechanical impurities in the residue-containing dirty oil in various ways, for example, a way of combining heating, filtering and/or centrifuging can be adopted. If the dirty oil is relatively high in mechanical impurities or heavy components, the pre-treatment may include centrifugation. In the manner of combining heating, filtering and/or centrifuging, the order and the number of times of heating, filtering and centrifuging are not particularly limited, and the residue-containing dirty oil may be heated first, filtered and centrifuged, or the residue-containing dirty oil may be filtered and centrifuged first and then heated, or the residue-containing dirty oil may be heated after heating, filtering and centrifuging, and so on.
In the scheme of the invention, the extraction treatment can be completed by one-stage extraction or multi-stage extraction.
In one embodiment of the invention, the extraction treatment is only provided with primary extraction, and the primary extraction process comprises the steps of fully mixing the residue-containing dirty oil with mechanical impurities removed, light oil and water, and performing settlement separation after mixing; the light oil and water in the intensive mixing are the light oil and water obtained by the evaporation; and settling and separating to obtain sewage and extracted sump oil, discharging the sewage, and evaporating the extracted sump oil.
In one embodiment of the invention, the extraction treatment is provided with multiple stages of extraction, and each stage of extraction comprises the steps of fully mixing the residue-containing dirty oil with mechanical impurities removed, light oil and water, and performing settlement separation after mixing; in the full mixing of each stage of extraction, the light oil is the light oil obtained by evaporation, and the water is the water obtained by the next stage of treatment. That is, in the thorough mixing of the first stage extraction, the light oil is the light oil obtained by the evaporation, and the water is the water obtained by the settling separation of the next stage extraction; in the full mixing of the last stage of extraction, the light oil is the light oil obtained by the evaporation, and the water is the water obtained by the evaporation; meanwhile, the extracted dirty oil obtained by the settling separation of the last stage of extraction is sent to be evaporated, and the water obtained by the settling separation of the first stage of extraction is discharged as sewage.
In the scheme of the invention, the full mixing in the extraction can be realized by adopting various existing devices, such as a Venturi mixer or a static mixer, and also can adopt other mixing devices; the present invention preferably employs a static mixer to achieve said thorough mixing.
In the scheme of the invention, the sedimentation separation in the extraction can be realized by adopting various existing devices, such as a tower or a tank, and the sedimentation separation is preferably realized by adopting the tank.
In a preferred embodiment of the present invention, in order to better separate the emulsified oil from the residual-containing dirty oil, it is preferable that a certain proportion of an auxiliary agent is added while the residual-containing dirty oil from which mechanical impurities are removed is fully mixed with the light oil and the water in the extraction treatment, wherein the auxiliary agent includes a mixture of any two or more of a bidirectional demulsifier, a demetallizing agent and a charge neutralizer.
The bidirectional demulsifier is a mixture of a forward agent and a reverse agent, can demulsify and separate most of emulsion in the dirty oil, gradually enlarges suspended matter particles to form flocs, and accelerates sedimentation separation; the preferred positive-working agent of the present invention contains at least one selected from the group consisting of polyoxypropylene polyoxyethylene ethers, phenol-amine resins, and polyepichlorohydrin polycondensates, or a mixture of two or more thereof, and polyoxypropylene polyoxyethylene ethers are more preferred. The preferred reversal agent of the invention at least contains one or a mixture of more than two of polyacrylamide (liquid and solid), polyaluminium chloride and polyaluminium ferric silicate, more preferably polyacrylamide, and most preferably liquid polyacrylamide.
The demetallization agent can transfer metal cations in the macromolecular organic acid salt forming the intractable emulsion into the water phase; the preferable demetallizing agent at least contains a mixture of any two or more of hydroxyethylidene diphosphonic acid, citric acid, formic acid, glacial acetic acid, hydrochloric acid or nitric acid; more preferably a mixture of any two or more of hydroxyethylidene diphosphonic acid, formic acid, glacial acetic acid, hydrochloric acid or nitric acid.
The charge neutralizer can enable anions in the dirty oil to interact with the cationic surfactant to destroy the hydrophilic and oleophilic properties of the dirty oil to form an oil-soluble high molecular organic matter and be fused into an oil phase, so that the purified solid residue generated by the high molecular organic matter is eliminated; the preferred charge neutralizer of the invention at least contains the mixture of any two or more of octadecyl polyoxyethylene ether, polyethylene glycol ester or polyol fatty acid ester; more preferably a mixture of octadecyl polyoxyethylene ether and polyethylene glycol ester.
In a further preferable scheme of the invention, in the extraction treatment, the proportion of the two-way demulsifier added into the sump oil is 500-3000ppm in terms of the weight ratio of the two-way demulsifier to the sump oil; the proportion of the demetallizing agent added into the dirty oil is 1000-5000 PPM in terms of the weight ratio of the demetallizing agent to the dirty oil; the proportion of the charge neutralizer added into the dirty oil is 10-100ppm according to the weight ratio of the charge neutralizer to the dirty oil.
Compared with the prior art, the invention has the following beneficial effects:
1. closed operation without VOCs generation
The whole purification process of the invention is continuously and hermetically operated, VOCs can not be generated, and the strictest requirements of safety and environmental protection specifications can be met.
2. Good oil-water separation effect and no generation of solid waste and hazardous waste
In the purification process, a two-phase extractant containing light oil and water is used, so that water-soluble inorganic salt and insoluble inorganic solid impurities in the dirty oil enter a water-phase decontamination water treatment plant, and the water content in the purified oil can meet the requirements of trace, inorganic salt and heavy metal on catalysis or coking; the insoluble organic solid enters the oil phase and is sent to the catalytic or coking processing of a refinery, and the history that the purification of the residue-containing dirty oil must generate waste solid and hazardous waste is broken through.
3. Good demulsification effect of extraction
In the preferred process of the invention, the extraction adopts a two-phase extractant containing light oil and water for demulsification, and is also assisted by a two-way demulsifier, a charge neutralizer, a demetalization and other compound additives, so that the oil-water demulsification and separation capability is greatly improved.
4. Self-extraction saves resources and energy consumption
Light oil and water in the two-phase extractant are both obtained from the treatment process, so that self-extraction is realized, resources are saved, repeated processing of the extractant is avoided, and energy consumption is further saved.
In a word, the oil and water produced by the purification process of the oil stain containing slag has better quality, short flow, low investment, low operation cost, low labor intensity, safe and environment-friendly working environment and no waste slag polluting the environment.
Drawings
FIG. 1 is a flow chart of the self-extraction purification process of the dirty oil containing dregs with two-stage extraction in example 1.
FIG. 2 is a flow chart of the self-extraction purification process of the dirty oil containing dregs and provided with only one stage of extraction in example 2.
Detailed Description
The invention provides a self-extraction purification process of residue-containing dirty oil, which comprises the following steps of continuously treating the residue-containing dirty oil under a closed condition:
1) Pre-processing unit
Pretreating the dirty oil containing the slag in a mode of combining heating, filtering and centrifuging to remove part of mechanical impurities; the equipment mainly comprises heating equipment, filtering equipment and centrifugal equipment, wherein the heating aims to reduce the viscosity of the dirty oil and promote efficient filtering, and the temperature of the heating equipment is controlled to be between 30 and 80 ℃ after heating, and is preferably higher than 35 ℃; the heating device may take a variety of forms. The filtering equipment can remove a small amount of solid impurities in the dirty oil, and is selected from one or more of a tubular filter, a basket filter, a rotary vibration sieve, a linear sieve, a swinging sieve, an ultrasonic vibration sieve, a straight-line sieve and a plate-frame filter, preferably the tubular filter or the basket filter. The centrifugal equipment can be one or more of a three-phase separator, a two-phase separator, a screw stacking machine or a hydrocyclone. The heating device, the filtering device and the centrifugal device can be freely combined;
2) Extraction unit
Adding two-phase extractant (light oil and water) and auxiliary agent (bidirectional demulsifier, demetallizing agent and charge neutralizer) into the dirty oil without mechanical impurities, and performing extraction treatment at 80-130 deg.C under 0-1.5Mpa to obtain sewage and extracted dirty oil; the initial phase of the two-phase extractant in the step comes from the outside of the system, and the subsequent evaporation unit is used after the process is continuously operated and stabilized;
the extraction unit can be internally provided with one-stage or multi-stage extraction, and each stage of extraction comprises a full mixing process of an extraction reagent and dirty oil and a settling separation process after full mixing. Therefore, the equipment of the extraction unit comprises mixing equipment and extraction separation equipment, wherein the mixing equipment can be a static mixer, a Venturi mixer, a stirring kettle or a plate tower; the separation apparatus may be a column or a tank.
Mixing and extracting the sump oil added with the two-phase extractant and the auxiliary agent by a mixing device, then feeding the sump oil into a separation device, settling and separating, then feeding harmful impurities in the sump oil into a sump water phase in the form of water-soluble salt and inorganic impurities, discharging the sump oil from the bottom of the separation device to a sewage system outside the system, and feeding the extracted sump oil containing organic impurities and a small amount of water to an evaporation unit;
3) Evaporation unit
And (3) the sump oil after extraction enters an evaporation unit, the evaporation equipment mainly comprises evaporation equipment, a cooler and an oil-water separation tank, the evaporation equipment is a distillation kettle, the evaporation temperature is controlled to be between 60 and 180 ℃, and the pressure is controlled to be between-0.09 and 0.5 Mpa. The heat source of the evaporation unit can be low-pressure steam, medium-pressure steam, a low-temperature heat source of a refinery plant or a hot process medium. After evaporation, the components at the top of the distillation kettle are condensed by a cooler, uncondensed gas is sent to a flare line, the condensed components are separated into light oil and water by an oil-water separation tank, and the light oil and the water which are used as extractant components are respectively returned to the extraction of 2) for reuse through different pumps and pipelines; and the qualified purified oil at the bottom is cooled by the cooler and then is pumped to a downstream device outside the system for application. The water content in the purified oil can be adjusted at will according to the requirements of downstream devices, and even can reach the trace level.
After the treatment by the process, the water content in the purified dirty oil can be marked, the oil content in water is less than 100ppm, the chloride ion content in the purified dirty oil is less than or equal to 10mg/L, and the metal ion content in the oil can reach the following level: the content of copper ions is less than or equal to 10.00mg/Kg, the content of iron ions is less than or equal to 200mg/Kg, the content of sodium ions is less than or equal to 10mg/Kg, the content of nickel ions is less than or equal to 8mg/Kg, and the content of vanadium ions is less than or equal to 1mg/Kg. According to the metal pollution index formula of the catalyst, the content of metal ions in the purified oil has little influence on the catalyst of the catalytic cracking unit, and the requirement of entering the catalytic cracking unit is met.
Example 1.
The two-phase two-stage self-extraction purification of the residue-containing dirty oil in the petrochemical tank area of the major China Petroleum Port is carried out by adopting a process, the process flow is shown in figure 1, and the specific steps and the flow are as follows:
1) Conveying the dirty oil containing the residues to a pretreatment unit through a pipeline by a tank area dirty oil pump, heating to 62 ℃ by heating equipment, and filtering by a basket filter to remove partial mechanical impurities such as sand particles, rust and the like;
2) The pretreated dirty oil is sent into a self-extraction unit through a pipeline, and is fully mixed with light oil from an evaporation unit, washing water from a secondary self-extraction settling tank and an auxiliary agent (a bidirectional demulsifier added according to the proportion of 1500ppm of the pretreated dirty oil, a demetallizing agent added according to the proportion of 3000ppm of the pretreated dirty oil and a charge neutralizing agent added according to the proportion of 50ppm of the pretreated dirty oil) in a primary self-extraction static mixer, heated and then enters the primary self-extraction settling tank for settling for 2 hours, and the mixture is subjected to sedimentation demulsification separation at 80 ℃ and 0.2MPa to obtain the primary self-extracted dirty oil and sewage; and discharging the sewage to a sewage treatment system.
3) Sending the first-stage self-extracted dirty oil obtained in the step 2) into a second-stage self-extracted static mixer, fully mixing the first-stage self-extracted dirty oil with light oil and water from an evaporation unit, then sending the mixture into a second-stage self-extracted settling tank, performing extraction, settling and separation for 2 hours at 80 ℃ and 0.2Mpa to obtain layered demetallized dirty oil and washing water, and returning the washing water to the first-stage self-extracted static mixer;
4) Feeding the demetallized dirty oil obtained in the step 3) into a distillation still of an evaporation unit, evaporating at 130 ℃ and under 0.5Mpa, and recovering light oil, water and purified qualified oil with the water content less than or equal to 1%. And delivering the purified qualified oil with qualified water content to a downstream device.
5) Separating the light oil obtained in the step 4) into two paths for recycling to the static mixer in the steps 2) and 3); recycling the water obtained in the step 4) to the static mixer of the secondary self-extraction in the step 3).
Example 2.
The two-phase one-stage self-extraction purification of the residue-containing dirty oil in the petrochemical tank area of the major China Petroleum Port is carried out by adopting a process, the process flow is shown in figure 2, and the specific steps and the flow are as follows:
1) Conveying the dirty oil containing the residues to a pretreatment unit through a pipeline by a tank area dirty oil pump, heating to 75 ℃ by heating equipment, and filtering by a basket filter and carrying out centrifugal treatment by a three-phase machine to remove partial mechanical impurities such as sand and stone particles, iron rust and the like;
2) The pretreated dirty oil is sent into a self-extraction unit through a pipeline, and is fully mixed with light oil, water and a bidirectional demulsifier which are added according to the proportion of 1500ppm of the pretreated dirty oil from an evaporation unit, a demetallizing agent which is added according to the proportion of 3000ppm of the pretreated dirty oil and a charge neutralizer which is added according to the proportion of 50ppm of the pretreated dirty oil in a self-extraction static mixer, the mixture is heated and then enters a self-extraction settling tank to settle for 2 hours, and the mixture is subjected to settling, demulsification and separation at 100 ℃ and 1.0Mpa to obtain the self-extracted dirty oil and sewage; and discharging the sewage to a sewage treatment system.
3) Sending the self-extracted dirty oil obtained in the step 2) into a distillation still of an evaporation unit, evaporating at 150 ℃ and 0.2Mpa, and recovering light oil, water and purified qualified oil with the water content less than or equal to 1%. The purified qualified oil with qualified water content is sent out to a downstream device.
4) Recycling the light oil and water obtained in the step 3) to the self-extracting static mixer in the step 2) through a pump and a pipeline respectively.
Claims (14)
1. A self-extraction purification process of slag-containing dirty oil in the refining industry comprises the steps of continuously pretreating, extracting and evaporating the slag-containing dirty oil under a closed condition; the method specifically comprises the following steps: removing part of mechanical impurities from the dirty oil containing the residues through pretreatment; adding light oil and water into the dirty oil with part of mechanical impurities removed, and simultaneously adding an auxiliary agent for extraction treatment to obtain sewage and extracted dirty oil; evaporating the extracted dirty oil to obtain light oil, water and purified oil; the light oil and water obtained by evaporation are reused for the extraction treatment; the proportion of the light oil added into the sump oil is 0.5 to 1.5 in terms of the weight ratio of the light oil to the sump oil; the amount of water added into the dirty oil is 1 to 4 according to the weight ratio of water to dirty oil; the auxiliary agent comprises a mixture of any two or more of a bidirectional demulsifier, a demetallization agent or a charge neutralizer, wherein the bidirectional demulsifier is a mixture of a forward agent and a reverse agent; the forward agent at least contains one or a mixture of more than two of polyoxypropylene polyoxyethylene ether, phenolic amine resin or polyepichlorohydrin polycondensate, and the reverse agent at least contains one or a mixture of more than two of liquid polyacrylamide, solid polyacrylamide, polyaluminium chloride and polyaluminium ferric silicate; the extraction treatment is carried out for 2-5h under the conditions of 80-130 ℃ and 0-1.5Mpa, the evaporation temperature is controlled to be 60-180 ℃ and the pressure is controlled to be-0.09-0.5 Mpa.
2. The process of claim 1, wherein: the proportion of the light oil to the sump oil is 0.5 to 1 according to the weight ratio of the light oil to the sump oil.
3. The process of claim 1, wherein: the amount of water added into the dirty oil is 1 to 2 according to the weight ratio of water to dirty oil.
4. The process of claim 1, wherein the extraction treatment is only provided with a primary extraction, and the primary extraction process comprises the following steps: fully mixing the residue-containing dirty oil with the mechanical impurities removed, light oil, water and an auxiliary agent, and performing sedimentation separation after mixing; the light oil and water in the intensive mixing are the light oil and water obtained by the evaporation; the auxiliary agent comprises a mixture of any two or more of a bidirectional demulsifier, a demetallization agent or a charge neutralizer, wherein the bidirectional demulsifier is a mixture of a forward agent and a reverse agent; the forward agent at least contains one or a mixture of more than two of polyoxypropylene polyoxyethylene ether, phenolic amine resin or polyepichlorohydrin polycondensate, and the reverse agent at least contains one or a mixture of more than two of liquid polyacrylamide, solid polyacrylamide, polyaluminium chloride and polyaluminium ferric silicate; and settling and separating to obtain sewage and extracted sump oil, discharging the sewage, and evaporating the extracted sump oil.
5. The process of claim 1, wherein said extraction process comprises a plurality of stages, each stage comprising: fully mixing the residue-containing dirty oil with mechanical impurities removed with light oil, water and an auxiliary agent, and performing settlement separation after mixing; in the full mixing of each stage of extraction, the light oil is the light oil obtained by evaporation, and the water is the water obtained by the next stage of treatment; that is, in the thorough mixing of the first stage extraction, the light oil is the one obtained by the evaporation, and the water is the one obtained by the settling separation of the next stage extraction; in the full mixing of the last stage of extraction, the light oil is the light oil obtained by the evaporation, and the water is the water obtained by the evaporation; meanwhile, the extracted dirty oil obtained by the settling separation of the last stage of extraction is sent to be evaporated, and the water obtained by the settling separation of the first stage of extraction is discharged as sewage; the auxiliary agent comprises a mixture of any two or more of a bidirectional demulsifier, a demetallization agent or a charge neutralizer, wherein the bidirectional demulsifier is a mixture of a forward agent and a reverse agent; the forward agent at least contains one or a mixture of more than two of polyoxypropylene polyoxyethylene ether, phenolic amine resin or polyepichlorohydrin polycondensate, and the reverse agent at least contains one or a mixture of more than two of liquid polyacrylamide, solid polyacrylamide, polyaluminium chloride and polyaluminium ferric silicate.
6. The process of any one of claims 4 or 5, wherein the thorough mixing in the extraction is achieved using a static mixer.
7. The process of any one of claims 4 or 5, wherein the settling separation in the extraction is achieved using a settling tank.
8. The process of claim 1, wherein: the forward agent is polyoxypropylene polyoxyethylene ether; the reversal agent is liquid polyacrylamide or solid polyacrylamide.
9. The process of claim 1, wherein: the reversal agent is liquid polyacrylamide.
10. The process of claim 1, wherein: the demetallization agent at least contains the mixture of any two of hydroxyethylidene diphosphonic acid, citric acid, formic acid, glacial acetic acid, hydrochloric acid or nitric acid.
11. The process of claim 1, wherein: the demetallization agent is a mixture of more than two of hydroxyethylidene diphosphonic acid, formic acid, glacial acetic acid, hydrochloric acid or nitric acid.
12. The process of claim 1, wherein: the charge neutralizer at least contains a mixture of more than two of octadecyl polyoxyethylene ether, polyethylene glycol ester or polyol fatty acid ester.
13. The process of claim 1, wherein: the charge neutralizer is a mixture of octadecyl polyoxyethylene ether and polyethylene glycol ester.
14. The process of any one of claims 1 to 5, 8 to 13, wherein: in the extraction treatment, the proportion of the two-way demulsifier added into the sump oil is 500-3000ppm according to the weight ratio of the two-way demulsifier to the sump oil; the proportion of the demetallizing agent added into the sump oil is 1000-5000 ppm by weight of the demetallizing agent and the sump oil; the proportion of the charge neutralizer added into the dirty oil is 10-100ppm according to the weight ratio of the charge neutralizer to the dirty oil.
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| CN101984028A (en) * | 2010-10-29 | 2011-03-09 | 湖南农业大学 | High-oryzanol rice bran oil two-phase extraction de-acidification refining technology |
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