CN110669582A - Method for eluting salt from waste animal and vegetable oil fiber membrane water and process system thereof - Google Patents
Method for eluting salt from waste animal and vegetable oil fiber membrane water and process system thereof Download PDFInfo
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- CN110669582A CN110669582A CN201910905690.8A CN201910905690A CN110669582A CN 110669582 A CN110669582 A CN 110669582A CN 201910905690 A CN201910905690 A CN 201910905690A CN 110669582 A CN110669582 A CN 110669582A
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- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B3/00—Refining fats or fatty oils
- C11B3/001—Refining fats or fatty oils by a combination of two or more of the means hereafter
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- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B3/00—Refining fats or fatty oils
- C11B3/006—Refining fats or fatty oils by extraction
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- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B3/00—Refining fats or fatty oils
- C11B3/008—Refining fats or fatty oils by filtration, e.g. including ultra filtration, dialysis
Abstract
The invention discloses a method for eluting salt from waste animal and vegetable oil fiber membrane water and a process system thereof, wherein the waste animal and vegetable oil is filtered and heated, and then is washed by at least one stage of fiber membrane water together with a demetallizing agent, a dechlorinating agent and a demulsifier along with washing water, and the desalting of the washed waste animal and vegetable oil is finished; the operation period of the device is prolonged, and the energy consumption of the device is reduced.
Description
Technical Field
The invention belongs to the technical field of biomass grease pretreatment processes, and particularly relates to a pretreatment method for producing a biological liquid fuel by using waste animal and vegetable grease (containing waste cooking oil) as a raw material, in particular to a method for eluting salt from waste animal and vegetable grease fiber membrane water and a process system thereof.
Background
The biological liquid fuel is prepared by processing aquatic plant oil and fat such as oil crops, wild oil plants, engineering microalgae and the like, animal oil and fat, catering waste oil and the like serving as raw materials, has low sulfur content, does not contain aromatic hydrocarbon, is environment-friendly, can reduce the emission of particulate matters, carbon dioxide and sulfur dioxide compared with petroleum diesel oil, is a clean energy source, has the advantages of reproducibility, rich raw materials, replaceability, lower cost and the like, and is particularly urgent for the double pressure of economic rapid development and environmental protection and the acceleration of the industrialization process of high-efficiency clean biological liquid fuel.
The waste animal and vegetable oil is an important raw material for developing biological liquid fuel in China at present, and due to the fact that the waste animal and vegetable oil is complex in source, contains a large amount of salt and chlorine and is seriously emulsified, metal content is usually hundreds of micrograms per gram, even thousands of micrograms per gram, total chlorine content is usually dozens of micrograms per gram, and the total chlorine content can reach hundreds of micrograms per gram, the long-period operation of a subsequent processing device is seriously influenced, and potential safety hazards are buried in a subsequent hydrogenation system.
Chinese patent application publication No. CN105368580A discloses a method for removing organic chloride from waste cooking oil, which comprises performing at least one stage of electric desalting on the waste cooking oil, adding a dechlorinating agent for dechlorinating, and performing electric desalting on the reactant after the dechlorinating reaction to obtain the waste cooking oil with organic chloride removed.
Chinese patent No. CN104974789B discloses a pretreatment method of waste cooking oil and a method for preparing alkane by hydrodeoxygenation of waste cooking oil, wherein the pretreatment dechlorination method comprises the steps of reacting ① lower alcohol with the waste cooking oil under the condition of ester exchange reaction, and carrying out demulsification and dehydration on a reaction product obtained in the step ① under the condition of demulsification and dehydration by ② to obtain the treated waste cooking oil.
The food waste oil pretreatment method has the following problems in practice that ① does not remove dissolved oxygen in the food waste oil, so that pipelines, a heat exchanger, a heating furnace, a reactor and the like are seriously coked under a high-temperature condition, the long-period operation of a device is influenced, ② food waste oil is complex in source, contains a surfactant, is unclear in an oil-water interface in an electric field, is unstable in electric desalting operation, and is high in energy consumption of multiple electric desalting processes, ③ is high in metal and chlorine content in the food waste oil processed at present, only a demulsifier or a dechlorinating agent is added, and then electric desalting is carried out, the electric desalting effect cannot be guaranteed, and the energy consumption of the multi-stage electric desalting process is high.
How to remove salt and chlorine in waste animal and vegetable oil with high efficiency and low cost is a technical problem to be solved urgently. Therefore, the research of removing harmful impurities such as salt, chlorine and the like in the pretreatment of the waste animal and vegetable oil is developed to form a stable and efficient pretreatment method of the biological liquid fuel raw material and ensure the stable operation of the subsequent hydrogenation process.
Disclosure of Invention
Aiming at the technical defects of the existing waste animal and vegetable oil pretreatment process, the invention aims to provide a waste animal and vegetable oil fiber membrane water salt elution method and a process system thereof, wherein at least one stage of fiber membrane water washing desalination is adopted, and a demulsifier, a demetallization agent and a dechlorination agent are added in an auxiliary manner, so that the purpose of waste animal and vegetable oil pretreatment is achieved, the harm of harmful impurities such as salt, chlorine and the like to a subsequent processing device can be solved, and the coking and corrosion of equipment and pipelines are avoided; the operation period of the device is prolonged, and the energy consumption of the device is reduced.
In order to achieve the purpose, the invention adopts the following technical scheme:
a method for eluting salt from waste animal and vegetable oil fiber membrane water is characterized in that: filtering and heating the waste animal and vegetable oil, washing the waste animal and vegetable oil, the demetallization agent, the dechlorination agent and the demulsifier together with washing water through at least one stage of fiber membrane, and desalting the washed waste animal and vegetable oil.
Furthermore, the waste animal and vegetable oil is washed by a secondary fiber membrane, and the specific washing process is as follows: the waste animal and vegetable oil and fat, the demetallization agent and/or the dechlorination agent and the washing water are washed by a first-stage fiber membrane together, the demulsifier and/or the dechlorination agent and the waste animal and vegetable oil and fat washed by the first-stage fiber membrane together enter a second-stage fiber membrane for washing, and the desalting is finished by the waste animal and vegetable oil and fat washed by the second-stage fiber membrane.
Furthermore, the heating temperature of the waste animal and vegetable oil is 120-150 ℃.
Furthermore, the operation temperature of fiber membrane washing is 120-150 ℃; the operating pressure is 0.6-1.5 MPa.
Furthermore, the addition amount of the demulsifier is 10-50 mug/g of the sum of the waste animal and vegetable oil and water.
Furthermore, the ratio of the added mass of the demetallizing agent to the sum of the contents of iron, calcium and magnesium in the waste animal and vegetable oil is 2-5: 1.
furthermore, the mass of the dechlorinating agent added is 1-5 times of the chlorine content in the raw material waste animal and vegetable oil.
The utility model provides a useless animal and vegetable oil fibrous membrane water elution salt process system which characterized in that: comprises a filtering system, a heating device and at least one stage of fiber membrane washing system which are connected in sequence;
the fiber membrane washing system comprises a fiber membrane contactor and a settling tank, wherein the fiber membrane contactor and the settling tank are communicated from top to bottom, a raw material inlet is formed in the upper portion of the fiber membrane contactor, a raw material outlet is formed in the top of the settling tank, an emulsification oil discharging port is formed in the middle lower portion of the settling tank, and a sewage draining port is formed in the bottom of the settling tank.
Furthermore, the fiber membrane washing system comprises a first-stage fiber membrane washing system and a second-stage fiber membrane washing system,
the first-stage fiber membrane washing system comprises a first-stage fiber membrane contactor and a first-stage settling tank, the second-stage fiber membrane washing system comprises a second-stage fiber membrane contactor and a second-stage settling tank, and a raw material outlet of the first-stage settling tank is communicated with a raw material inlet of the second-stage fiber membrane contactor;
the fiber membrane washing system further comprises a washing circulating pump, and the washing circulating pump is arranged between a sewage draining outlet of the second-stage settling tank and a raw material inlet of the first-stage fiber membrane contactor.
Furthermore, an emulsified oil layer observation window is arranged on the settling tank.
The principle of the method of the invention is as follows:
1. the fiber membrane has a demulsification effect on water-in-oil emulsified oil, and the fiber membrane has a wetting coalescence effect on an external phase and an extrusion shearing effect on an external force, so that the deformation coalescence of the external phase preferentially passes through the fiber membrane, the deformation and the breakage of the external phase cause the probability of contact, collision and coalescence of inner phase liquid drops, larger liquid drops are formed, and then the emulsion is unstable in oil-water separation.
2. The waste animal and vegetable oil and fat can be settled and separated from a water phase at 120-150 ℃, and the density difference can realize settlement separation when the waste animal and vegetable oil and fat and water are heated to 120-150 ℃.
3. Under the condition of auxiliary addition of proper amounts of demulsifier, demetallization agent and dechlorination agent, the water washing desalination of the fiber membrane can achieve the expected effect.
Due to the adoption of the technical scheme, the invention has the following beneficial effects:
1) the method adopts a fiber membrane washing technology, utilizes the demulsification performance of the fiber membrane, assists the action of adding the demulsifier, the demetallizing agent and the dechlorinating agent, and combines the oil-water density difference under certain conditions to wash and settle to remove harmful impurities such as salt, chlorine and the like in the waste animal and vegetable oil, so that the desalting and dechlorinating efficiency can be improved, and the using amount of auxiliary additives can be reduced, thereby avoiding the harm caused by the harmful impurities in the subsequent processing process when the waste animal and vegetable oil is used as a biological liquid fuel raw material.
2) The method adopts the fiber membrane for washing and sedimentation, avoids adopting a waste animal and vegetable oil and water washing mixer, avoids the risk of further emulsification of oil and water, and reduces the dosage of the demulsifier.
3) The method of the invention adopts fiber membrane washing sedimentation, does not adopt an electric desalting technology, and plays a role in energy conservation and consumption reduction.
4) The middle part of the settling tank is provided with an emulsified oil layer observation window and an emulsified oil discharge port, when the emulsified oil layer is accumulated in the settling tank, the emulsified oil layer is timely discharged, and the effects of washing, settling, desalting and dechlorinating of the fiber membrane are ensured.
Drawings
FIG. 1 is a schematic view of a process flow of water washing desalination of waste animal and vegetable oil fiber membrane;
in the figure: 1. a filtration system; 11. a first stage filter; 12. a second stage filter; 13. a third stage filter; 2. a heating device; 3. a fiber membrane water washing system; 31. a first-stage fiber membrane washing system; 311. a first stage fiber membrane contactor; 312. a first stage settling tank; 32. a second-stage fiber membrane water washing system; 321. a second stage fiber membrane contactor; 322. a second stage settling tank; 33. washing the circulating pump with water; 34. a raw material inlet; 35. a raw material outlet; 36. an emulsion oil outlet; 37. a sewage draining port; 38. and (5) an emulsified oil layer observation window.
Detailed Description
In order that the present invention may be more readily and clearly understood, a more particular description of the invention briefly described above will be rendered by reference to specific embodiments that are illustrated in the appended drawings.
As shown in figure 1, a method for eluting salt from waste animal and vegetable oil fiber membrane water specifically comprises the following steps: filtering and heating the waste animal and vegetable oil, washing the waste animal and vegetable oil, the demetallization agent, the dechlorination agent and the demulsifier together with washing water through at least one stage of fiber membrane, and desalting the washed waste animal and vegetable oil.
In the application, the waste animal and vegetable oil filtration adopts three-stage filtration, namely pre-filtration and a filter screen with the filtration precision of 20-30 meshes; filtering with active carbon or semi-coke, wherein the filtering precision is 30-40 meshes; fine filtration, wherein the filtration precision of the fine filter is more than 98 percent of the removal rate of particles with the particle size of 25 mu m.
Preferably, the fine filtration is a sintered metal fiber microporous filter or a wedge-section metal screen.
The operating temperature in the filtering process is 70-90 ℃, and the operating pressure is 0.5-1.5 MPa.
In the application, the heating temperature of the waste animal and vegetable oil is 120-150 ℃. The waste animal and vegetable oil and fat can be settled and separated from a water phase at 120-150 ℃, and the density difference can realize settlement separation when the waste animal and vegetable oil and fat and water are heated to 120-150 ℃.
In this application, useless animal and vegetable fat is through second grade fiber membrane washing, and specific washing process is: the waste animal and vegetable oil and fat, the demetallization agent and/or the dechlorination agent and the washing water are washed by a first-stage fiber membrane together, the demulsifier and/or the dechlorination agent and the waste animal and vegetable oil and fat washed by the first-stage fiber membrane together enter a second-stage fiber membrane for washing, and the desalting is finished by the waste animal and vegetable oil and fat washed by the second-stage fiber membrane.
Preferably, the water washing water is softened water or deoxygenated water.
Preferably, the fibrous membrane is a hydrophilic fibrous membrane.
In the application, the volume ratio of the water quantity of the washing water to the waste animal and vegetable oil is 0.1-0.3.
In the application, the operation temperature of fiber membrane washing is 120-150 ℃; the operating pressure is 0.6-1.5 MPa.
Preferably, the operation temperature of the waste animal and vegetable oil entering a fiber membrane washing system is 120-150 ℃; the operating pressure is 0.6-1.0 MPa. The operation temperature of the washing water entering a fiber membrane washing system is 120-150 ℃; the operating pressure is 0.8-1.5 MPa.
The retention time of the waste animal and vegetable oil in the fiber membrane washing system is 10-30 minutes, when the thickness of an emulsified oil layer in the fiber membrane washing system is increased to more than 300mm, the emulsified oil is discharged from the fiber membrane washing system, so that the fiber membrane washing effect is ensured.
In the application, the main component of the demulsifier is a polymer with the molecular weight of 1000-10000, such as: the addition amount of the non-ionic polyoxyethylene polyoxypropylene ether and the demulsifier is 10-50 mu g/g of the sum of the waste animal and vegetable oil and water.
In the present application, the main component of the demetallizing agent is an organic acid, such as: one or more of oxalic acid, phosphoric acid, formic acid and ethylene diamine tetraacetic acid. The ratio of the added mass of the demetallizing agent to the sum of the contents of iron, calcium and magnesium in the waste animal and vegetable oil is 2-5: 1.
in the present application, the main component of the dechlorinating agent is a metal salt of an alcohol, such as: one or more of potassium methoxide, potassium ethoxide, sodium methoxide, potassium isopropoxide and potassium tert-butoxide. The mass of the dechlorinating agent added is 1-5 times of the chlorine content in the raw material waste animal and vegetable oil.
A waste animal and vegetable oil fiber membrane water salt elution process system comprises a filtering system 1, a heating device 2 and at least one stage of fiber membrane washing system 3 which are connected in sequence.
The filtration system 1 includes a first stage filter 11, a second stage filter 12, and a third stage filter 13.
The first-stage filter 11 is pre-filtering and adopts a filter screen with the precision of 20-30 meshes; the second-stage filter 12 is activated carbon or semi-coke filtration and adopts a filter screen with the precision of 30-40 meshes; the third filter 13 is fine filtration, and the fine filter is adopted, so that the filtration precision reaches more than 98 percent of the removal rate of particles with the particle size of 25 mu m.
Preferably, the third stage filter 13 is a sintered metal fiber microporous filter or a wedge-section metal screen.
The operating temperature in the filtering process is 70-90 ℃, and the operating pressure is 0.5-1.5 MPa.
The heating device 2 is a raw oil heater.
Preferably, the raw oil heater adopts a shell-and-tube heat exchanger taking steam as a heating medium, the shell-side material is waste animal and vegetable oil, and the tube side is low-pressure steam of 1.0 MPa.
Fiber membrane water washing system 3 includes fiber membrane contactor and settling cask, and fiber membrane contactor and settling cask top-down intercommunication set up, and fiber membrane contactor upper portion is equipped with raw materials entry 34, and the settling cask top is equipped with raw materials export 35, and the well lower part is equipped with row emulsification hydraulic fluid port 36, and the bottom is equipped with sewage outlet 37.
The waste animal and vegetable oil after being washed and desalted enters a raw material settling tank to remove most of free water, then is sent to a dehydrating tower for vacuum dehydration and dissolved oxygen, and then enters a waste animal and vegetable oil olefin removal, metal removal, degreasing, acid prevention and dechlorination system.
In this application, fibre membrane washing system 3 includes first order fibre membrane washing system 31 and second level fibre membrane washing system 32, and first order fibre membrane washing system 31 includes first order fibre membrane contactor 311 and first order settling cask 312, and second level fibre membrane washing system 32 includes second level fibre membrane contactor 321 and second level settling cask 322, and the raw materials export 35 of first order settling cask 312 communicates with the raw materials entry 34 of second level fibre membrane contactor 321.
The fiber membrane washing system 3 further comprises a washing circulating pump 33, and the washing circulating pump 33 is arranged between the sewage draining outlet 37 of the second-stage settling tank 322 and the raw material inlet 34 of the first-stage fiber membrane contactor 311.
The flow of the water washing water in the system is as follows: the water washing water enters from the raw material inlet 34 of the second-stage fiber membrane contactor 321, flows out from the sewage discharge port 37 of the second-stage settling tank 322, enters from the raw material inlet 34 of the first-stage fiber membrane contactor 311 through the water washing circulating pump, and flows out from the sewage discharge port 37 of the first-stage settling tank 312.
The flow of the waste animal and vegetable oil in the system is as follows: the waste animal and vegetable oil enters from a raw material inlet 34 of the first-stage fiber membrane contactor 311, is washed by the first-stage fiber membrane washing system 31 for desalination, flows out from a raw material outlet 35 of the first-stage settling tank 312, enters from a raw material inlet 34 of the second-stage fiber membrane contactor 321, is washed by the second-stage fiber membrane washing system 32 for desalination, and flows out from a raw material outlet 35 of the second-stage settling tank 322.
In this application, be equipped with emulsion oil reservoir observation window 38 on the settling cask.
When the emulsified oil layer in the settling tank thickens to more than 300mm, the emulsified oil is discharged from the emulsified oil discharge port 36 on the settling tank, so that the water washing effect of the fiber membrane contactor is ensured.
The process flow of the waste animal and vegetable oil fiber membrane water-eluting salt comprises the following steps:
waste animal and vegetable oil raw materials from a tank area are subjected to three-stage filtration including pre-filtration, activated carbon or semi-coke filtration and fine filtration, and heated by a raw oil heater, and then enter a first-stage fiber membrane contactor 311 together with washing water added with a demetallizing agent or/and a dechlorinating agent to be in downstream contact; then, oil-water separation is carried out in the first-stage settling tank 312, an oil phase is led out from a raw material outlet 35 at the top of the first-stage settling tank 312, and enters the second-stage fiber membrane contactor 321 together with water washing water added with a demulsifier or/and a dechlorinating agent for downstream contact; then, the oil and water are separated in the second stage settling tank 322, and the oil phase is sent to the raw material settling tank from the raw material outlet 35 at the top of the second stage settling tank 322.
The washing water from the water drum of the second stage settling tank 322 is pressurized and circulated to the first stage fiber membrane contactor 311 by the washing circulating pump 33. The water-washed water is discharged from the first-stage settling tank 312 to a sewage treatment plant.
When the thickness of the emulsified oil layer gathered in the first-stage settling tank 312 and the second-stage settling tank 322 reaches 300mm, the emulsified oil is discharged from the emulsified oil discharging ports 36 on the first-stage settling tank 312 and the second-stage settling tank 322 in time.
Example 1
Carrying out three-stage filtration on waste animal and vegetable oil raw materials from a tank area, wherein a filter screen with the filtering precision of 20 meshes is adopted for pre-filtration; the active carbon or semi-coke filtration adopts a filter screen with 30-mesh filtration precision; the fine filtration adopts a sintered metal fiber microporous filter, and the filtration precision reaches more than 98 percent of the removal rate of 25 mu m particles. The operation temperature is 70 ℃, and the operation pressure is 1.1 MPa.
The fiber membrane is a hydrophilic fiber membrane, the washing water adopts deoxygenated water, and the volume ratio of the washing water entering the fiber membrane contactor to the waste animal and vegetable oil raw material entering the fiber membrane contactor is 0.3. The operation temperature of the waste animal and vegetable oil entering the first-stage fiber membrane contactor 311 is 120 ℃, and the operation pressure is 0.7 MPa; the operation temperature of the washing water entering the first-stage washing fiber membrane contactor 311 is 120 ℃, and the operation pressure is 1.0 MPa. The operation temperature of the waste animal and vegetable oil entering the second-stage fiber membrane contactor 321 is 120 ℃, and the operation pressure is 0.6 MPa; the washing water enters the second-stage fiber membrane contactor 321, the operating temperature is 120 ℃, and the operating pressure is 0.8 MPa.
The residence time of the first stage water wash settling tank 312 and the second stage water wash settling tank 322 is 10 minutes.
When the thickness of the emulsified oil layer in the first-stage washing settling tank 312 and the second-stage washing settling tank 322 is increased to more than 300mm, the emulsified oil is discharged from the emulsified oil discharge ports 36 on the first-stage washing settling tank 312 and the second-stage washing settling tank 322.
The addition amount of the demulsifier is 10 mug/g of the sum of the water washing amount of the waste animal and vegetable oil and fat.
The ratio of the added mass of the demetallization agent to the sum of the contents of iron, calcium and magnesium in the waste animal and vegetable oil is 2: 1.
The mass of the dechlorinating agent added is 1 time of the chlorine content in the raw material waste animal and vegetable oil.
After the fiber membrane is washed, the salt content in the waste animal and vegetable oil is less than 3mg/L, the chlorine removal rate of the waste animal and vegetable oil reaches more than 65 percent (by mass), and the chlorine content in the waste animal and vegetable oil is less than 5 mg/L.
Example 2
Carrying out three-stage filtration on waste animal and vegetable oil raw materials from a tank area, wherein a filter screen with the filtering precision of 20 meshes is adopted for pre-filtration; the active carbon or semi-coke filtration adopts a filter screen with 30-mesh filtration precision; the fine filtration adopts a sintered metal fiber microporous filter, and the filtration precision reaches more than 98 percent of the removal rate of 25 mu m particles. The operation temperature is 70 ℃, and the operation pressure is 1.0 MPa.
The fiber membrane is a hydrophilic fiber membrane, the washing water adopts deoxygenated water, and the volume ratio of the washing water entering the fiber membrane contactor to the waste animal and vegetable oil raw material entering the fiber membrane contactor is 0.1. The operation temperature of the waste animal and vegetable oil entering the first-stage fiber membrane contactor 311 is 120 ℃, and the operation pressure is 0.7 MPa; the operation temperature of the washing water entering the first-stage washing fiber membrane contactor 311 is 120 ℃, and the operation pressure is 1.0 MPa. The operation temperature of the waste animal and vegetable oil entering the second-stage fiber membrane contactor 321 is 120 ℃, and the operation pressure is 0.6 MPa; the washing water enters the second-stage fiber membrane contactor 321, the operating temperature is 120 ℃, and the operating pressure is 0.8 MPa.
The residence time of the first stage water wash settling tank 312 and the second stage water wash settling tank 322 was 30 minutes.
When the thickness of the emulsified oil layer in the first-stage washing settling tank 312 and the second-stage washing settling tank 322 is increased to more than 300mm, the emulsified oil is discharged from the emulsified oil discharge ports 36 on the first-stage washing settling tank 312 and the second-stage washing settling tank 322.
The addition amount of the demulsifier is 10 mug/g of the sum of the water washing amount of the waste animal and vegetable oil and fat.
The ratio of the added mass of the demetallization agent to the sum of the contents of iron, calcium and magnesium in the waste animal and vegetable oil is 2: 1.
The mass of the dechlorinating agent added is 5 times of the chlorine content in the raw material waste animal and vegetable oil.
After the fiber membrane is washed, the salt content in the waste animal and vegetable oil is less than 3mg/L, the chlorine removal rate of the waste animal and vegetable oil reaches over 75 percent (by mass), and the chlorine content in the waste animal and vegetable oil is less than 3 mg/L.
Example 3
Carrying out three-stage filtration on waste animal and vegetable oil raw materials from a tank area, wherein a filter screen with the filtering precision of 20 meshes is adopted for pre-filtration; the active carbon or semi-coke filtration adopts a filter screen with 30-mesh filtration precision; the fine filtration adopts a sintered metal fiber microporous filter, and the filtration precision reaches more than 98 percent of the removal rate of 25 mu m particles. The operation temperature is 70 ℃, and the operation pressure is 1.0 MPa.
The fiber membrane is a hydrophilic fiber membrane, the washing water adopts deoxygenated water, and the volume ratio of the washing water entering the fiber membrane contactor to the waste animal and vegetable oil raw material entering the fiber membrane contactor is 0.2. The operation temperature of the waste animal and vegetable oil entering the first-stage fiber membrane contactor 311 is 120 ℃, and the operation pressure is 0.7 MPa; the operation temperature of the washing water entering the first-stage washing fiber membrane contactor 311 is 120 ℃, and the operation pressure is 1.0 MPa. The operation temperature of the waste animal and vegetable oil entering the second-stage fiber membrane contactor 321 is 120 ℃, and the operation pressure is 0.6 MPa; the washing water enters the second-stage fiber membrane contactor 321, the operating temperature is 120 ℃, and the operating pressure is 0.8 MPa.
The residence time of the first stage water wash settling tank 312 and the second stage water wash settling tank 322 is 20 minutes.
When the thickness of the emulsified oil layer in the first-stage washing settling tank 312 and the second-stage washing settling tank 322 is increased to more than 300mm, the emulsified oil is discharged from the emulsified oil discharge ports 36 on the first-stage washing settling tank 312 and the second-stage washing settling tank 322.
The addition amount of the demulsifier is 10 mug/g of the sum of the water washing amount of the waste animal and vegetable oil and fat.
The ratio of the added mass of the demetallization agent to the sum of the contents of iron, calcium and magnesium in the waste animal and vegetable oil is 5: 1.
The mass of the dechlorinating agent added is 2 times of the chlorine content in the raw material waste animal and vegetable oil.
After the fiber membrane is washed, the salt content in the waste animal and vegetable oil is less than 2mg/L, the chlorine removal rate of the waste animal and vegetable oil reaches more than 70 percent (by mass), and the chlorine content in the waste animal and vegetable oil is less than 5 mg/L.
Example 4
Carrying out three-stage filtration on waste animal and vegetable oil raw materials from a tank area, wherein a filter screen with the filtering precision of 20 meshes is adopted for pre-filtration; the active carbon or semi-coke filtration adopts a filter screen with 30-mesh filtration precision; the fine filtration adopts a sintered metal fiber microporous filter, and the filtration precision reaches more than 98 percent of the removal rate of 25 mu m particles. The operation temperature is 90 ℃, and the operation pressure is 1.5 MPa.
The fiber membrane is a hydrophilic fiber membrane, the washing water adopts deoxygenated water, and the volume ratio of the washing water entering the fiber membrane contactor to the waste animal and vegetable oil raw material entering the fiber membrane contactor is 0.3. The operation temperature of the waste animal and vegetable oil entering the first-stage fiber membrane contactor 311 is 150 ℃, and the operation pressure is 1.0 MPa; the operation temperature of the washing water entering the first-stage washing fiber membrane contactor 311 is 150 ℃, and the operation pressure is 1.5 MPa. The operation temperature of the waste animal and vegetable oil entering the second-stage fiber membrane contactor 321 is 150 ℃, and the operation pressure is 0.8 MPa; the washing water enters the second-stage fiber membrane contactor 321, the operating temperature is 150 ℃, and the operating pressure is 1.0 MPa.
The residence time of the first stage water wash settling tank 312 and the second stage water wash settling tank 322 is 10 minutes.
When the thickness of the emulsified oil layer in the first-stage washing settling tank 312 and the second-stage washing settling tank 322 is increased to more than 300mm, the emulsified oil is discharged from the emulsified oil discharge ports 36 on the first-stage washing settling tank 312 and the second-stage washing settling tank 322.
The addition amount of the demulsifier is 10 mug/g of the sum of the water washing amount of the waste animal and vegetable oil and fat.
The ratio of the added mass of the demetallization agent to the sum of the contents of iron, calcium and magnesium in the waste animal and vegetable oil is 2: 1.
The mass of the dechlorinating agent added is 1 time of the chlorine content in the raw material waste animal and vegetable oil.
After the fiber membrane is washed, the salt content in the waste animal and vegetable oil is less than 2mg/L, the chlorine removal rate of the waste animal and vegetable oil reaches more than 65 percent (by mass), and the chlorine content in the waste animal and vegetable oil is less than 5 mg/L.
Example 5
Carrying out three-stage filtration on waste animal and vegetable oil raw materials from a tank area, wherein a filter screen with the filtering precision of 20 meshes is adopted for pre-filtration; the active carbon or semi-coke filtration adopts a filter screen with 30-mesh filtration precision; the fine filtration adopts a sintered metal fiber microporous filter, and the filtration precision reaches more than 98 percent of the removal rate of 25 mu m particles. The operation temperature is 90 ℃, and the operation pressure is 1.5 MPa.
The fiber membrane is a hydrophilic fiber membrane, the washing water adopts deoxygenated water, and the volume ratio of the washing water entering the fiber membrane contactor to the waste animal and vegetable oil raw material entering the fiber membrane contactor is 0.1. The operation temperature of the waste animal and vegetable oil entering the first-stage fiber membrane contactor 311 is 150 ℃, and the operation pressure is 1.0 MPa; the operation temperature of the washing water entering the first-stage washing fiber membrane contactor 311 is 150 ℃, and the operation pressure is 1.5 MPa. The operation temperature of the waste animal and vegetable oil entering the second-stage fiber membrane contactor 321 is 150 ℃, and the operation pressure is 0.8 MPa; the washing water enters the second-stage fiber membrane contactor 321, the operating temperature is 150 ℃, and the operating pressure is 1.0 MPa.
The residence time of the first stage water wash settling tank 312 and the second stage water wash settling tank 322 was 30 minutes.
When the thickness of the emulsified oil layer in the first-stage washing settling tank 312 and the second-stage washing settling tank 322 is increased to more than 300mm, the emulsified oil is discharged from the emulsified oil discharge ports 36 on the first-stage washing settling tank 312 and the second-stage washing settling tank 322.
The addition amount of the demulsifier is 10 mug/g of the sum of the water washing amount of the waste animal and vegetable oil and fat.
The ratio of the added mass of the demetallization agent to the sum of the contents of iron, calcium and magnesium in the waste animal and vegetable oil is 2: 1.
The mass of the dechlorinating agent added is 2 times of the chlorine content in the raw material waste animal and vegetable oil.
After the fiber membrane is washed, the salt content in the waste animal and vegetable oil is less than 2mg/L, the chlorine removal rate of the waste animal and vegetable oil reaches more than 70 percent (by mass), and the chlorine content in the waste animal and vegetable oil is less than 4 mg/L.
Example 6
Carrying out three-stage filtration on waste animal and vegetable oil raw materials from a tank area, wherein a filter screen with the filtering precision of 20 meshes is adopted for pre-filtration; the active carbon or semi-coke filtration adopts a filter screen with 30-mesh filtration precision; the fine filtration adopts a sintered metal fiber microporous filter, and the filtration precision reaches more than 98 percent of the removal rate of 25 mu m particles. The operation temperature is 90 ℃, and the operation pressure is 1.5 MPa.
The fiber membrane is a hydrophilic fiber membrane, the washing water adopts deoxygenated water, and the volume ratio of the washing water entering the fiber membrane contactor to the waste animal and vegetable oil raw material entering the fiber membrane contactor is 0.1. The operation temperature of the waste animal and vegetable oil entering the first-stage fiber membrane contactor 311 is 150 ℃, and the operation pressure is 1.0 MPa; the operation temperature of the washing water entering the first-stage washing fiber membrane contactor 311 is 150 ℃, and the operation pressure is 1.5 MPa. The operation temperature of the waste animal and vegetable oil entering the second-stage fiber membrane contactor 321 is 150 ℃, and the operation pressure is 0.8 MPa; the washing water enters the second-stage fiber membrane contactor 321, the operating temperature is 150 ℃, and the operating pressure is 1.0 MPa.
The residence time of the first stage water wash settling tank 312 and the second stage water wash settling tank 322 is 20 minutes.
When the thickness of the emulsified oil layer in the first-stage washing settling tank 312 and the second-stage washing settling tank 322 is increased to more than 300mm, the emulsified oil is discharged from the emulsified oil discharge ports 36 on the first-stage washing settling tank 312 and the second-stage washing settling tank 322.
The addition amount of the demulsifier is 10 mug/g of the sum of the water washing amount of the waste animal and vegetable oil and fat.
The ratio of the added mass of the demetallization agent to the sum of the contents of iron, calcium and magnesium in the waste animal and vegetable oil is 2: 1.
The mass of the dechlorinating agent added is 5 times of the chlorine content in the raw material waste animal and vegetable oil.
After the fiber membrane is washed, the salt content in the waste animal and vegetable oil is less than 2mg/L, the chlorine removal rate of the waste animal and vegetable oil reaches over 75 percent (by mass), and the chlorine content in the waste animal and vegetable oil is less than 3 mg/L.
The above embodiments are described in further detail to solve the technical problems, technical solutions and advantages of the present invention, and it should be understood that the above embodiments are only examples of the present invention and are not intended to limit the present invention, and any modifications, equivalent substitutions, improvements and the like made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A method for eluting salt from waste animal and vegetable oil fiber membrane water is characterized in that: filtering and heating the waste animal and vegetable oil, washing the waste animal and vegetable oil, the demetallization agent, the dechlorination agent and the demulsifier together with washing water through at least one stage of fiber membrane, and desalting the washed waste animal and vegetable oil.
2. The method for eluting salt from waste animal and vegetable oil fiber membrane water according to claim 1, characterized in that: washing waste animal and vegetable oil with a secondary fiber membrane, wherein the specific washing process is as follows: the waste animal and vegetable oil and fat, the demetallization agent and/or the dechlorination agent and the washing water are washed by a first-stage fiber membrane together, the demulsifier and/or the dechlorination agent and the waste animal and vegetable oil and fat washed by the first-stage fiber membrane together enter a second-stage fiber membrane for washing, and the desalting is finished by the waste animal and vegetable oil and fat washed by the second-stage fiber membrane.
3. The method for eluting salt from waste animal and vegetable oil fiber membrane water according to claim 1, characterized in that: the heating temperature of the waste animal and vegetable oil is 120-150 ℃.
4. The method for eluting salt from waste animal and vegetable oil fiber membrane water according to claim 1, characterized in that: the operation temperature of fiber membrane washing is 120-150 ℃; the operating pressure is 0.6-1.5 MPa.
5. The method for eluting salt from waste animal and vegetable oil fiber membrane water according to claim 1, characterized in that: the addition amount of the demulsifier is 10-50 mug/g of the sum of the waste animal and vegetable oil and the water washing amount.
6. The method for eluting salt from waste animal and vegetable oil fiber membrane water according to claim 1, characterized in that: the ratio of the added mass of the demetallizing agent to the sum of the contents of iron, calcium and magnesium in the waste animal and vegetable oil is 2-5: 1.
7. the method for eluting salt from waste animal and vegetable oil fiber membrane water according to claim 1, characterized in that: the mass of the dechlorinating agent added is 1-5 times of the chlorine content in the raw material waste animal and vegetable oil.
8. The utility model provides a useless animal and vegetable oil fibrous membrane water elution salt process system which characterized in that: comprises a filtering system (1), a heating device (2) and at least one stage of fiber membrane water washing system (3) which are connected in sequence;
fiber membrane rinse-system (3) are including fiber membrane contactor and settling cask, fiber membrane contactor and settling cask top-down intercommunication set up, fiber membrane contactor upper portion is equipped with raw materials entry (34), the settling cask top is equipped with raw materials export (35), and well lower part is equipped with row's emulsification hydraulic fluid port (36), and the bottom is equipped with drain (37).
9. The waste animal and vegetable oil fiber membrane water-elution salt process system of claim 8, wherein: the fiber membrane washing system (3) comprises a first-stage fiber membrane washing system (31) and a second-stage fiber membrane washing system (32), the first-stage fiber membrane washing system (31) comprises a first-stage fiber membrane contactor (311) and a first-stage settling tank (312), the second-stage fiber membrane washing system (32) comprises a second-stage fiber membrane contactor (321) and a second-stage settling tank (322), and a raw material outlet (35) of the first-stage settling tank (312) is communicated with a raw material inlet (34) of the second-stage fiber membrane contactor (321);
fiber membrane water washing system (3) still includes washing circulating pump (33), washing circulating pump (33) set up between blow off mouth of a river (37) of second grade settling cask (322) and raw materials entry (34) of first order fiber membrane contactor (311).
10. The waste animal and vegetable oil fiber membrane water-elution salt process system of claim 8, wherein: and an emulsified oil layer observation window (38) is arranged on the settling tank.
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