CN212610501U

CN212610501U - Rapid deacidification and low-sulfur high-yield production system for producing fuel oil by using waste animal and vegetable oil

Info

Publication number: CN212610501U
Application number: CN202021740999.0U
Authority: CN
Inventors: 徐兴
Original assignee: Sichuan Jinshang Environmental Protection Technology Co ltd
Current assignee: Sichuan Jinshang Environmental Protection Technology Co ltd
Priority date: 2020-08-19
Filing date: 2020-08-19
Publication date: 2021-02-26
Anticipated expiration: 2030-08-19

Abstract

The utility model discloses a abandonment animal and vegetable fat production fuel falls sour and low sulphur high yield production system fast, solves the technical problem that prior art abandonment animal and vegetable fat production living beings fuel yield is low. The system comprises a pretreatment system, a reaction kettle, a waste oil conveying pipe, a hydrogen peroxide conveying pipe, a first cleaning water conveying pipe, a first jacket heater, a stirrer, a three-phase centrifuge A, a flash evaporation drying tower, a rapid deacidification system, a high-pressure reaction kettle, a separation tank, an atmospheric deacidification system, an atmospheric reaction kettle, an alcohol precipitation tower and a pure methanol liquid storage tank; a second jacket heater, a high-pressure reaction kettle material pipe, a four-way valve A, a liquid methanol conveying pipe, a raw oil conveying pipe and an overhauling and cleaning pipe are arranged in the high-pressure reaction kettle; the normal pressure reaction kettle is provided with a third jacket heater, a first grease outward conveying pipe, a second methanol outward conveying pipe, a normal pressure reaction kettle material pipe, a four-way valve B and a methanol conveying pipe. The utility model discloses can effectively improve abandonment animal and vegetable oil production living beings fuel yield.

Description

Rapid deacidification and low-sulfur high-yield production system for producing fuel oil by using waste animal and vegetable oil

Technical Field

The utility model belongs to the technical field of abandonment animal and vegetable fat recovery processing application production facility, concretely relates to abandonment animal and vegetable fat production fuel falls sour and low sulfur high yield production system fast.

Background

In the production process of edible oil, a large amount of acidified waste oil can be produced, the acidified waste oil can be used for producing biomass fuel oil from waste animal and vegetable oil, however, after the acidified waste oil is primarily filtered, the acidified waste oil also contains a large amount of salts, pigments and colloids, the colloids mainly exist in the form of starch, the salts contain a large amount of organic chloride and organic sulfur salt, the organic chloride and the organic sulfur salt can not be removed from the oil by adopting the traditional washing method, meanwhile, the acidified waste oil has high content of fatty acid, the content of the fatty acid can reach about 140, the traditional deacidification method is adopted, the deacidification efficiency is low, the deacidification effect is not ideal, the content of the fatty acid can only be reduced from 140 to 5-10, the difficulty of subsequent processes is increased, the subsequent ester exchange rate can be reduced, the distillation efficiency of biomass fuel oil produced from mouth-shaped waste animal and vegetable oil due to high content is low, finally, the yield of biomass fuel oil produced by waste animal and vegetable oil is low.

Therefore, the utility model discloses a abandonment animal and vegetable fat production fuel falls sour and low sulphur high yield production system fast, at the preliminary treatment stage, fills into among the acidizing waste oil and fat to wash water and subside from top injection washing water after filling into hydrogen peroxide solution oxidation, oxidizes organochlorine salt and organosulfur salt out CL^-And S^2-Washing with water and settling to make the oil contain CL^-Less than 30ppm of salts and containing S^2-The salt content is lower than 30ppm, in the process of reducing acid, firstly adopting an autoclave to react the grease with liquid methanol to reduce the fatty acid content in the grease from 140 to 5-10, then adopting a normal pressure kettle to react the grease with vapor methanol, then carrying out alcohol precipitation and sedimentation to reduce the fatty acid content in the grease from 5-10 to within 1, and finally outputting the grease from an alcohol precipitation tower, wherein the fatty acid content is within 1, the water content is within 0.5 percent, and the grease contains CL^-Less than 30ppm of salts and containing S^2-The salt content is lower than 30ppm, and after the grease enters an ester exchange system, the ester exchange rate can be effectively improved and the grease can be obtained later than that obtained by the traditional deacidification method due to less colloid and other impuritiesThe distillation efficiency is continued, and the yield of the biomass fuel oil produced by the waste animal and vegetable oil can be improved by 10-20 percent.

SUMMERY OF THE UTILITY MODEL

The to-be-solved technical problem of the utility model is: the system for producing the fuel oil by the waste animal and vegetable oil and the low-sulfur high-yield production is provided, and the technical problems that the subsequent ester exchange rate is low and the distillation efficiency is low due to low deacidification efficiency and unsatisfactory deacidification effect when the acidified waste oil and the waste vegetable oil are subjected to deacidification treatment in the prior art, and the yield of the biomass fuel oil produced by the waste animal and vegetable oil and the waste animal and vegetable oil is unsatisfactory are solved.

In order to achieve the above object, the utility model adopts the following technical scheme:

the system for producing fuel oil by using waste animal and vegetable oil and fat to quickly reduce acid and reduce sulfur and has high yield comprises a pretreatment system, a quick acid reduction system connected out of the pretreatment system and a normal pressure acid reduction system connected out of the quick acid reduction system;

the pretreatment system comprises a reaction kettle, a waste oil conveying pipe which is connected to the reaction kettle and used for injecting acidified waste oil into the reaction kettle, a hydrogen peroxide conveying pipe which is connected to the reaction kettle and used for injecting hydrogen peroxide into the reaction kettle, a first cleaning water conveying pipe which is connected to the reaction kettle and used for injecting cleaning water into the reaction kettle, a first jacket heater which is arranged on the reaction kettle, a stirrer which is arranged in the reaction kettle, a three-phase centrifuge A which is used for performing three-phase separation of slag, oil and water on slag oil settled in the reaction kettle and is connected out of the reaction kettle through a slag oil conveying pipe, and a flash drying tower which is used for performing dehydration treatment on settled supernatant oil liquid in the reaction kettle and is connected out of the reaction kettle through a first oil conveying pipe; a material discharging pipe is arranged at the bottom of the reaction kettle and is respectively connected with the slag oil conveying pipe and the first oil conveying pipe, the flash drying tower is connected with a vacuum pump, and the flash drying tower is connected with a raw oil conveying pipe;

the quick deacidification system comprises a high-pressure reaction kettle and a separation tank which is connected with the upper part of the high-pressure reaction kettle through a conveying pipe and is used for separating fuel and methanol after reaction, a second jacket heater is arranged in the high-pressure reaction kettle, the bottom of the high-pressure reaction kettle is communicated with a material pipe of the high-pressure reaction kettle, a four-way valve A is connected on the material pipe of the high-pressure reaction kettle, the remaining three interfaces on the four-way valve A are respectively connected with a liquid methanol conveying pipe for filling liquid methanol into the high-pressure reaction kettle, a raw oil conveying pipe for filling raw oil into the high-pressure reaction kettle, an overhaul cleaning pipe for discharging materials during shutdown overhaul and filling cleaning water into the high-pressure reaction kettle, a pressure reducing valve is arranged on the conveying pipe, the top of the separation tank is connected with a first methanol external conveying pipe, the first methanol external conveying pipe is connected to a condensation recovery system, the first oil output pipe is connected to a normal-pressure deacidification system;

the normal-pressure deacidification system comprises a normal-pressure reaction kettle, an alcohol separation tower and a pure methanol liquid storage tank, wherein the alcohol separation tower is connected out of the normal-pressure reaction kettle through a second oil material conveying pipe and is used for separating oil and water methanol through natural sedimentation; a third jacket heater is arranged on the normal pressure reaction kettle, a first grease outward conveying pipe for conveying grease with 5-10 fatty acid content in the normal pressure reaction kettle is connected on the normal pressure reaction kettle, a second methanol outward conveying pipe for discharging methanol gas outward is connected on the normal pressure reaction kettle, the first grease outward conveying pipe and the second methanol outward conveying pipe are connected on the top of the normal pressure reaction kettle, a normal pressure reaction kettle material pipe is connected on the bottom of the normal pressure reaction kettle, a four-way valve B is connected on the outlet of the normal pressure reaction kettle material pipe, one interface of the four-way valve B is connected with an inlet of the second oil conveying pipe, one interface of the four-way valve B is connected with a methanol conveying pipe for conveying methanol gas in the normal pressure reaction kettle, a pure methanol liquid storage tank is connected with a vaporizer through a pure methanol liquid conveying pipe, the inlet of the methanol conveying pipe is connected with the outlet of the vaporizer, the second methanol outward, the top of the alcohol separation tower is connected with a second oil outward conveying pipe, the second oil outward conveying pipe is connected to an ester exchange system in the production system for producing the biomass fuel oil by using the waste animal and vegetable oil, the bottom of the alcohol separation tower is connected with a water-methanol outward conveying pipe, and the water-methanol outward conveying pipe is connected to a water-methanol circulation recovery system in the production system for producing the biomass fuel oil by using the waste animal and vegetable oil.

Furthermore, a first flowmeter and a first pump are arranged on the hydrogen peroxide conveying pipe, a second flowmeter and a second pump are arranged on the first cleaning water conveying pipe, a third pump is arranged on the waste oil conveying pipe, a first valve is arranged on the discharging pipe, a second valve and a fourth pump are arranged on the slag oil conveying pipe, and a third valve and a fifth pump are arranged on the first oil conveying pipe.

Furthermore, one outlet of the three-phase centrifuge A is connected with a secondary water washing tank for carrying out secondary water washing on the oil material separated from the settled slag oil material, and the other two outlets are respectively connected with a slag material harmless treatment system for carrying out harmless treatment on the slag material separated from the settled slag oil material and a sewage treatment system for carrying out harmless treatment on the sewage separated from the settled slag oil material.

Furthermore, the stirrer comprises a driving motor arranged on the reaction kettle, a stirring rod connected with a driving shaft of the driving motor and positioned in the reaction kettle, and stirring blades arranged on two sides of the stirring rod in a staggered manner, wherein resistance reducing holes are formed in the stirring blades, and the driving motor is a forward and reverse rotating motor.

Furthermore, a spray head is arranged at the discharge port of the feed delivery pipe and is positioned in the middle of the separation tank; an eighth valve, a first oil pump and a third flowmeter are arranged on the raw oil conveying pipe; a ninth valve, a second oil pump and a fourth flowmeter are arranged on the liquid methanol delivery pipe; the first methanol output pipe is provided with a fourth valve and an air pump.

Furthermore, a material outer discharge pipe and a second cleaning water conveying pipe are connected to the maintenance cleaning pipe, the material outer discharge pipe is connected to the material temporary storage tank, and the second cleaning water conveying pipe is connected out from the cleaning water tank.

Furthermore, a fifth valve is arranged on the overhauling and cleaning pipe, a sixth valve and a fourth oil pump are arranged on the material discharge pipe, and a seventh valve and a fifth oil pump are arranged on the second cleaning water conveying pipe.

Furthermore, a condenser for liquefying gaseous methanol in the second methanol output pipe into liquid methanol is arranged on the second methanol output pipe.

Furthermore, a tenth valve, an eighth pump and a fifth flow meter are arranged on the first grease output pipe; an eleventh valve, a second air pump and a sixth flowmeter are arranged on the methanol delivery pipe, and the second air pump is an air pump; a twelfth valve and a third air pump are arranged on the second methanol output pipe, and the third air pump is an air pump; a thirteenth valve and a ninth pump are arranged on the second oil conveying pipe; a fourteenth valve and a tenth pump are arranged on the pure methanol liquid conveying pipe; a fifteenth valve and a sixth pump are arranged on the second grease output pipe; and a sixteenth valve and a seventh pump are arranged on the water methanol delivery pipe.

Furthermore, a seventeenth valve is arranged on the material pipe of the normal-pressure reaction kettle, the rest interface of the four-way valve B is connected with a standby pipeline, and an eighteenth valve is arranged on the standby pipeline.

Compared with the prior art, the utility model discloses following beneficial effect has:

the utility model has the advantages of simple structure and scientific and reasonable design, convenient to use fills into in the acidizing waste oil and fat to wash water and subside from top injection washing water after hydrogen peroxide solution oxidation in the preliminary treatment stage, oxidizes organochlorine salt and organosulfur salt out CL^-And S^2-Washing with water and settling to make the oil contain CL^-Less than 30ppm of salts and containing S^2-The salt content is lower than 30ppm, in the process of reducing acid, firstly adopting an autoclave to react the grease with liquid methanol to reduce the fatty acid content in the grease from 140 to 5-10, then adopting a normal pressure kettle to react the grease with vapor methanol, then carrying out alcohol precipitation and sedimentation to reduce the fatty acid content in the grease from 5-10 to less than 1, and finally outputting the grease from an alcohol precipitation tower, wherein the fatty acid content is less than 1, the water content is less than 0.5 percent, and the grease contains CL^-Less than 30ppm of salts and containing S^2-The salt content is lower than 30ppm, and compared with the grease obtained by the traditional deacidification method, the grease obtained by the grease entering the ester exchange system can effectively improve the ester exchange rate, and finally the yield of biomass fuel oil produced by waste animal and vegetable grease can be improved by 10-20 percent.

Drawings

Fig. 1 is a system block diagram of the present invention.

Fig. 2 is a schematic structural view of the stirrer of the present invention.

Wherein, the names corresponding to the reference numbers are:

1-pretreatment system, 2-rapid deacidification system, 3-atmospheric deacidification system, 11-reaction kettle, 12-waste oil conveying pipe, 13-hydrogen peroxide conveying pipe, 14-first cleaning water conveying pipe, 15-first jacket heater, 16-slag oil conveying pipe, 17-three-phase centrifuge A, 18-first oil conveying pipe, 19-flash evaporation drying tower, 110-stirrer, 111-driving motor, 112-stirring rod, 113-stirring blade, 114-first flow meter, 115-first pump, 116-second flow meter, 117-second pump, 118-third pump, 119-discharge pipe, 120-first valve, 121-second valve, 122-third valve, 123-secondary water washing tank, 124-resistance reducing hole, 125-vacuum pump, 126-fourth pump, 127-fifth pump, 128-slag harmless treatment system, 129-sewage treatment system, 21-high-pressure reaction kettle, 22-separating tank, 23-second jacket heater, 24-high-pressure reaction kettle material pipe, 25-four-way valve A, 26-liquid methanol conveying pipe, 27-raw oil conveying pipe, 28-first methanol external conveying pipe, 29-first grease external conveying pipe, 210-conveying pipe, 211-pressure reducing valve, 212-spray head, 213-eighth valve, 214-first oil pump, 215-third flow meter, 216-ninth valve, 217-second oil pump, 218-fourth flow meter, 221-fourth valve, 222-air pump, 223-overhaul cleaning pipe, 224-material external discharge pipe, air pump, 223-overhaul cleaning pipe, 225-second cleaning water delivery pipe, 226-material temporary storage tank, 227-clean water tank, 228-fifth valve, 229-sixth valve, 230-fourth oil pump, 231-seventh valve, 232-fifth oil pump, 233-three-way valve, 31-normal pressure reaction kettle, 32-second oil delivery pipe, 33-alcohol precipitation tower, 35-third jacket heater, 36-second methanol output pipe, 37-normal pressure reaction kettle material pipe, 38-four-way valve B, 39-methanol delivery pipe, 310-pure methanol liquid storage tank, 311-pure methanol liquid delivery pipe, 312-vaporizer, 313-methanol storage tank, 314-condenser, 315-second grease output pipe, 316-water methanol output pipe, 317-tenth valve, 318-eighth pump, 319-fifth flow meter, 320-eleventh valve, 321-second air pump, 322-sixth flow meter, 323-twelfth valve, 324-third air pump, 325-thirteenth valve, 326-ninth pump, 327-fourteenth valve, 328-tenth pump, 329-fifteenth valve, 330-sixth pump, 331-sixteenth valve, 332-seventh pump, 333-seventeenth valve, 334-spare pipe and 335-eighteenth valve.

Detailed Description

In order to make the objects, technical solutions and advantages of the present invention more clearly understood, the present invention is further described in detail below with reference to the accompanying drawings. It is to be understood that the embodiments described are only some embodiments of the invention, and not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.

In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element referred to must have a specific orientation or be constructed and operated in a specific orientation, and thus, it should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.

In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; of course, mechanical connection and electrical connection are also possible; alternatively, they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood according to specific situations by those skilled in the art.

As shown in figures 1 and 2, the utility model provides a abandonment animal and vegetable fat production fuel falls sour and low sulfur high yield production system fast, including pretreatment system 1, from pretreatment system 1 the quick acid system 2 that falls who connects out to and from the quick acid system 3 that falls of ordinary pressure that falls that system 2 connects out. The utility model has the advantages of simple structure and scientific and reasonable design, convenient to use fills into in the acidizing waste oil and fat from after hydrogen peroxide solution oxidation at the preliminary treatment stageInjecting cleaning water into the top of the reactor to perform water washing and sedimentation, and oxidizing organic chloride and organic sulfate to obtain CL^-And S^2-Washing with water and settling to make the oil contain CL^-Less than 30ppm of salts and containing S^2-The salt content is lower than 30ppm, in the process of reducing acid, firstly adopting an autoclave to react the grease with liquid methanol to reduce the fatty acid content in the grease from 140 to 5-10, then adopting a normal pressure kettle to react the grease with vapor methanol, then carrying out alcohol precipitation and sedimentation to reduce the fatty acid content in the grease from 5-10 to less than 1, and finally outputting the grease from an alcohol precipitation tower, wherein the fatty acid content is less than 1, the water content is less than 0.5 percent, and the grease contains CL^-Less than 30ppm of salts and containing S^2-And the salt content is lower than 30ppm, and compared with the grease obtained by the traditional deacidification method, the grease obtained by the conventional deacidification method can effectively improve the ester exchange rate and the distillation efficiency, and finally the yield of biomass fuel oil produced by using the waste animal and vegetable grease can be improved by 10-20%.

The utility model discloses pretreatment systems 1 simple structure, design scientific and reasonable, convenient to use, the acidizing waste oil fat of having handled through this pretreatment equipment, water is miscellaneous to be less than 1%, unsaponifiable matter is less than 0.3%, contains CL^-Less than 30ppm of salts and S^2-The salt content is lower than 30ppm, the treated raw oil meets the production requirement of producing biomass fuel oil by using second-generation waste animal and vegetable oil, and the treatment efficiency and the yield can be improved. The pretreatment system 1 comprises a reaction kettle 11, a waste oil conveying pipe 12 connected to the reaction kettle 11 and used for injecting acidified waste oil into the reaction kettle 11, a hydrogen peroxide conveying pipe 13 connected to the reaction kettle 11 and used for injecting hydrogen peroxide into the reaction kettle 11, a first cleaning water conveying pipe 14 connected to the reaction kettle 11 and used for injecting cleaning water into the reaction kettle 11, a first jacket heater 15 arranged on the reaction kettle 11, a stirrer 110 arranged in the reaction kettle 11, a three-phase centrifuge A17 used for performing three-phase separation of slag, oil and water on slag oil settled in the reaction kettle 11 and a flash drying tower 19 used for performing dehydration treatment on the supernatant oil settled in the reaction kettle 11, wherein the slag oil conveying pipe 16 is connected from the reaction kettle 11 through a slag oil conveying pipe 16; a material discharging pipe 119 is arranged at the bottom of the reaction kettle 11, and the material discharging pipe 119 is respectively connected with the slag oil conveying pipe 16 and the first oil conveying pipe 18The flash drying tower 19 is connected with a vacuum pump 125, and the flash drying tower 19 is connected with a raw oil delivery pipe 27.

The utility model discloses be equipped with first flowmeter 114 and first pump 115 on the hydrogen peroxide solution conveyer pipe 13, be equipped with second flowmeter 116 and second pump 117 on the first washing water conveyer pipe 14, be equipped with third pump 118 on the waste oil conveyer pipe 12, be equipped with first valve 120 on arranging material pipe 119, be equipped with second valve 121 and fourth pump 126 on the sediment oil conveyer pipe 16, be equipped with third valve 122 and fifth pump 127 on the first oil conveyer pipe 18.

The utility model discloses an export of three-phase centrifuge A17 has connect and is used for carrying out the secondary washing's secondary washing jar 123 to the oil that separates from subsiding the sediment oil, and two surplus exports connect respectively to be used for carrying out innocent treatment's sediment material innocent treatment system and be used for carrying out innocent treatment's sewage treatment system to the sewage that separates from subsiding the sediment oil. The stirrer 110 comprises a driving motor 111 arranged on the reaction kettle 11, a stirring rod 112 connected with a driving shaft of the driving motor 111 and positioned in the reaction kettle 11, and stirring blades 113 arranged at two sides of the stirring rod 112 in a staggered manner, wherein resistance reducing holes 124 are arranged on the stirring blades 113, and the driving motor 111 is a forward and reverse rotating motor.

The utility model discloses pretreatment system 1 is during the operation, pour into the acidizing waste oil of pending through waste oil conveyer pipe in toward reation kettle, the acidizing waste oil can be the food and beverage waste oil of long-time rancidity, also can be the leftover bits of oil that produces in the edible oil production process, edible oil adds alkali (sodium hydroxide) and produces through the acidizing after improving fatty acid content, after having poured into the acidizing waste oil of pending processing, open first jacket heater and heat up to 80-90 ℃, through hydrogen peroxide solution conveyer pipe toward reation kettle in the hydrogen peroxide solution heavy 5-10% hydrogen peroxide solution of oil of injection, open the agitator stirring and make hydrogen peroxide solution react with waste oil after 2h, close the agitator, through first washing water conveyer pipe toward reation kettle in the injection heavy 5% washing water of oil subside 24-36h, washing water is from reation kettle internal top injection, make the washing water of injection from the top down subside washing, after the sedimentation is finished, the first valve and the second valve are firstly opened and the fourth pump is started to ensure that the slag at the bottom of the reaction kettle is leftThe oil is discharged firstly, the residue oil passes through a three-phase centrifuge A, wherein the oil enters a secondary water washing tank and is washed by common water to recover byproduct oil which is used for other purposes and does not participate in the production of biomass fuel oil from waste animal and vegetable oil, the residue and sewage respectively enter a residue harmless treatment system and a sewage treatment system in a biomass fuel oil production system from waste animal and vegetable oil for harmless treatment, and the sewage is recycled after being treated to save water sources. Observing the discharging process of the oil residue through a sight glass of the reaction kettle, closing the second valve and the fourth pump after the oil residue is discharged, opening the third valve and the fifth pump to ensure that the supernatant oil liquid in the reaction kettle enters a flash drying tower for dehydration, opening a vacuum pump to reduce the pressure in the flash drying tower to-0.08 million P to-0.09 million P in the process, wherein the water impurity of the oil material discharged from the flash drying tower is lower than 0.5 percent, the unsaponifiable material of the oil material is lower than 0.3 percent, and the oil material contains CL^-Less than 30ppm of salts and S^2-The salt content is lower than 30ppm, which meets the raw oil standard for producing biomass fuel oil by using secondary waste animal and vegetable oil. The stirring of mixer can improve the efficiency of hydrogen peroxide solution oxidation acidizing waste oil, and the resistance when the stirring paddle leaf falls and hinders the hole can reduce the mixer stirring, reduces the energy consumption.

The utility model discloses an add hydrogen peroxide solution and acid waste oil reaction in past reation kettle, can be effectively with organic CL salt and organic S salt oxidation to CL^-Salt and S^2-And after the salt is washed with water and settled, most of impurities such as CL salt, S salt, colloid and the like in the acidic waste oil can be removed, and the pretreatment effect is very ideal. The method has strong applicability and is suitable for wide popularization and application in the technical field.

The utility model discloses fast falling sour system 2 simple structure, design scientific and reasonable, convenient to use, it can effectively improve fatty acid and methyl alcohol reaction rate, improves and falls sour efficiency, reduces fatty acid content to 5-10 from about 140 simultaneously, guarantees that follow-up manufacturing procedure is high-efficient smooth and easy. The utility model discloses quick deacidification system 2 includes high pressure batch autoclave 21, and be connected with high pressure batch autoclave 21 upper portion through conveying pipeline 210 and be used for carrying out the knockout drum 22 that separates the oil after the reaction and methyl alcohol, be equipped with second jacket heater 23 in high pressure batch autoclave 21, high pressure batch autoclave 21 bottom intercommunication has high pressure batch autoclave material pipe 24, be connected with cross valve A25 on high pressure batch autoclave material pipe 24, the remaining three interface on cross valve A25 is connected with respectively is used for filling into liquid methyl alcohol conveyer pipe 26 of liquid methyl alcohol in the high pressure batch autoclave 21, be used for filling into the raw oil conveyer pipe 27 of raw oil in the high pressure batch autoclave 21, and be used for discharging the material outward and for filling into the maintenance scavenge pipe 223 of washing water in the high pressure batch autoclave 21 during the downtime maintenance, be equipped with relief pressure reducing valve 211 on the conveying pipeline 210, knockout drum 22 top is connected with first methyl alcohol outer delivery pipe 28, first methyl alcohol outer delivery pipe 28 inserts to condensation recovery, the bottom of the separation tank 22 is connected with a first grease output pipe 29, and the first grease output pipe 29 is connected to the atmospheric pressure deacidification system 3.

The discharge port of the feed delivery pipe 210 of the utility model is provided with a spray head 212, and the spray head 212 is positioned in the middle part in the separation tank 22; the raw oil delivery pipe 27 is provided with an eighth valve 213, a first oil pump 214 and a third flow meter 215; a ninth valve 216, a second oil pump 217 and a fourth flowmeter 218 are arranged on the liquid methanol delivery pipe 26; the first methanol delivery pipe 28 is provided with a fourth valve 221 and an air pump 222.

The utility model discloses overhaul and be connected with material outer calandria 224 on the scavenge pipe 223 and the second washs water conveying pipe 225, material outer calandria 224 inserts to the material jar 226 of keeping in, and the second washs water conveying pipe 225 and connects out from clean water tank 227. A fifth valve 228 is arranged on the maintenance cleaning pipe 223, a sixth valve 229 and a fourth oil pump 230 are arranged on the material discharging pipe 224, and a seventh valve 231 and a fifth oil pump 232 are arranged on the second cleaning water conveying pipe 225.

The utility model discloses falling sour system 2 fast and pouring into raw oil and liquid methyl alcohol into to high-pressure batch autoclave in the reaction, high-pressure batch autoclave in operating pressure be 0.4-0.5 megapascal, operating temperature be 120 and give good care to 140 ℃, so, liquid methyl alcohol exists with the liquid state in high-pressure batch autoclave, compare in gaseous state methyl alcohol, its and the contact surface of raw oil will greatly increased, can effectively improve reaction rate between the two, generally 6-10min can react and accomplish, efficiency obtains improving greatly. During the use, liquid methanol is injected from the bottom of the high-pressure reaction kettle through the liquid methanol delivery pipe, raw oil is injected from the bottom of the high-pressure reaction kettle through the raw oil delivery pipe, the raw oil and the liquid methanol are simultaneously injected into the high-pressure reaction kettle, the flow rate is displayed through the flowmeter to control and adjust the injection proportion of the raw oil and the liquid methanol, after the reaction is finished, the pressure reducing valve is opened to deliver a reaction mixture into the separation tank to separate out the methanol, wherein the methanol is recycled from the condensation recovery system through the first methanol output pipe, and the oil is delivered to the normal pressure acid reduction system 3 through the first oil output pipe.

The utility model discloses be connected with on the cross valve A and overhaul the scavenge pipe, overhaul the scavenge pipe and be connected with the outer calandria of material and the second washs the water conveying pipe, the outer calandria of material inserts to the material jar of keeping in, and the second washs the water conveying pipe and connects out from clean water tank. When the high-pressure reaction kettle needs to be stopped to be cleaned, the fifth valve, the sixth valve and the fourth oil pump are firstly opened, residual materials in the high-pressure reaction kettle are discharged to the material temporary storage tank through the material discharge pipe, then the sixth valve and the fourth oil pump are closed, and the seventh valve and the fifth oil pump are opened to spray cleaning water in the cleaning water tank into the high-pressure reaction kettle for maintenance and cleaning. And discharging the cleaned cleaning water into a material temporary storage tank.

The utility model discloses the sustainable sour reaction that falls of high pressure batch autoclave, knockout drum also can continuously carry out the separation operation, and 6-10min can accomplish a reaction to can fall fatty acid to 5-10 from 140, it falls sour reaction efficiency height, effectual, and the practicality is strong, is suitable for and widelys popularize and apply in this technical field.

The utility model discloses 3 sour system of ordinary pressure deacidification simple structure, design scientific and reasonable, convenient to use to go on deacidification at 5-10 grease to fatty acid content and handle, make its fatty acid content reduce to more than 1, thereby can effectively improve follow-up ester exchange rate, and then can effectively improve abandonment animal and vegetable fat production living beings fuel yield, and abandonment animal and vegetable fat production living beings fuel yield can improve 5-10 percentage points. The atmospheric pressure deacidification system 3 of the utility model comprises an atmospheric pressure reaction kettle 31, an alcohol separation tower 33 for separating oil and water methanol by natural sedimentation and a pure methanol liquid storage tank 310 which are connected out from the atmospheric pressure reaction kettle 31 through a second oil material conveying pipe 32; a third jacket heater 35 is arranged on the normal pressure reaction kettle 31, a first grease outward conveying pipe 29 for conveying grease with 5-10 fatty acid content in the normal pressure reaction kettle 31 is connected on the normal pressure reaction kettle 31, a second methanol outward conveying pipe 36 for discharging methanol gas is connected on the normal pressure reaction kettle 31, the first grease outward conveying pipe 29 and the second methanol outward conveying pipe 36 are connected on the top of the normal pressure reaction kettle 31, a normal pressure reaction kettle material pipe 37 is connected on the bottom of the normal pressure reaction kettle 31, the outlet of the normal pressure reaction kettle material pipe 37 is connected with a four-way valve B38, one interface of the four-way valve B38 is connected with the inlet of the second oil conveying pipe 32, one interface of the four-way valve B38 is connected with a methanol conveying pipe 39 for conveying methanol gas in the normal pressure reaction kettle 31, a pure methanol liquid storage tank 310 is connected with a vaporizer 312 through a pure methanol liquid conveying pipe 311, the inlet of, the second methanol outward conveying pipe 36 is connected to the methanol storage tank 313, the inlet of the liquid methanol conveying pipe 26 is connected with the methanol storage tank 313, the top of the alcohol analysis tower 33 is connected with the second grease outward conveying pipe 315, the second grease outward conveying pipe 315 is connected to an ester exchange system in the biomass fuel oil production system for producing waste animal and vegetable grease, the bottom of the alcohol analysis tower 33 is connected with the water methanol outward conveying pipe 316, and the water methanol outward conveying pipe 316 is connected to a water methanol recycling system in the biomass fuel oil production system for producing waste animal and vegetable grease.

The utility model discloses be equipped with on the second methanol defeated outside of tubes 36 and be used for liquefying the gaseous methanol into the condenser 314 of liquid methanol in the second methanol defeated outside of tubes 36. A seventeenth valve 333 is arranged on the material pipe 37 of the normal pressure reaction kettle, the rest interface of the four-way valve B38 is connected with a standby pipeline 334, and an eighteenth valve 335 is arranged on the standby pipeline 334.

The first grease discharging pipe 29 of the utility model is provided with a tenth valve 317, an eighth pump 318 and a fifth flow meter 319; the methanol delivery pipe 39 is provided with an eleventh valve 320, a second air pump 321 and a sixth flow meter 322, and the second air pump 321 is an air pump; a twelfth valve 323 and a third air pump 324 are arranged on the second methanol output pipe 36, and the third air pump 324 is an air pump; a thirteenth valve 325 and a ninth pump 326 are arranged on the second oil conveying pipe 32; a fourteenth valve 327 and a tenth pump 328 are arranged on the pure methanol liquid conveying pipe 311; a fifteenth valve 329 and a sixth pump 330 are arranged on the second grease output pipe 315; the water-methanol delivery pipe 316 is provided with a sixteenth valve 331 and a seventh pump 332.

The utility model disclosesThe normal pressure deacidification system 3 mainly comprises a normal pressure reaction kettle and an alcohol analysis tower, wherein the oil separated by the separation tank is injected into the normal pressure reaction kettle by a first oil external transmission pipe, the fatty acid content of the oil is 5-10, pure methanol gas is input into the normal pressure reaction kettle by a methanol transmission pipe, the injection amount of the oil and the pure methanol gas is controlled according to the flow displayed on a flow meter, the temperature in the normal pressure reaction kettle is increased to 110-plus-115 ℃ by a third jacket heater, the oil and the pure methanol gas react completely under the working condition of 110-plus-115 ℃ for 1h, the reacted mixture is transmitted into the alcohol analysis tower through a second oil transmission pipe for natural settling separation, the oil positioned at the upper layer of the alcohol analysis tower has the fatty acid content of more than 1, the water content of less than 0.5 percent and contains CL, and the oil positioned at the upper layer of^-Less than 30ppm of salts and containing S^2-The salt content is lower than 30ppm, and the salt is conveyed to an ester exchange system through a second grease output pipe to carry out ester exchange reaction, so that the yield of biomass fuel oil produced by waste animal and vegetable grease can be effectively improved by 10-20 percent. The water methanol (containing soaps, water, impurities and methanol) at the lower layer of the alcohol precipitation tower is connected to a water methanol recycling system through a water methanol output pipe to recycle the methanol. In the process, the methanol gas discharged from the second methanol delivery pipe is condensed into liquid methanol through a condenser (the condenser is a chilled water condenser) and stored in a methanol storage tank, and the liquid methanol in the methanol storage tank is conveyed into the high-pressure reaction kettle through a liquid methanol conveying pipe. The gaseous methanol in the methanol conveying pipe is obtained by vaporizing liquid pure methanol in a pure methanol liquid storage tank by a vaporizer.

The utility model discloses can effectively fall to the fatty acid content in the grease raw materials more than 1, moisture content falls to within 0.5%, so can effectively improve follow-up ester exchange rate, and then improve abandonment animal and vegetable grease production living beings fuel yield, its practicality is strong, is suitable for and widelys popularize and apply in this technical field.

Finally, it should be noted that: the above embodiments are only preferred embodiments of the present invention to illustrate the technical solution of the present invention, but not to limit the same, and certainly not to limit the scope of the present invention; although the present invention has been described in detail with reference to the foregoing embodiments, it should be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention; that is, the technical problems solved by the present invention are still consistent with the present invention, and all the modifications or colors made in the spirit and the idea of the main design of the present invention are included in the protection scope of the present invention; in addition, will the technical scheme of the utility model direct or indirect application is in other relevant technical field, all including on the same reason the utility model discloses an in the patent protection scope.

Claims

1. The system for producing fuel oil by using waste animal and vegetable oil and fat for quickly reducing acid and realizing low sulfur and high yield is characterized by comprising a pretreatment system (1), a quick acid reducing system (2) connected out of the pretreatment system (1) and a normal-pressure acid reducing system (3) connected out of the quick acid reducing system (2);

the pretreatment system (1) comprises a reaction kettle (11), a waste oil conveying pipe (12) which is connected to the reaction kettle (11) and used for injecting acidified waste oil into the reaction kettle (11), a hydrogen peroxide conveying pipe (13) which is connected to the reaction kettle (11) and used for injecting hydrogen peroxide into the reaction kettle (11), a first cleaning water conveying pipe (14) which is connected to the reaction kettle (11) and used for injecting cleaning water into the reaction kettle (11), a first jacket heater (15) arranged on the reaction kettle (11), and a stirrer (110) arranged in the reaction kettle (11), a three-phase centrifuge A (17) for separating slag, oil and water from the slag oil settled in the reaction kettle (11) is connected out of the reaction kettle (11) through a slag oil conveying pipe (16), and a flash evaporation drying tower (19) which is connected out from the reaction kettle (11) through a first oil material conveying pipe (18) and is used for dehydrating settled supernatant oil liquid in the reaction kettle (11); a material discharging pipe (119) is arranged at the bottom of the reaction kettle (11), the material discharging pipe (119) is respectively connected with the slag oil conveying pipe (16) and the first oil conveying pipe (18), the flash drying tower (19) is connected with a vacuum pump (125), and the flash drying tower (19) is connected with a raw oil conveying pipe (27);

the rapid deacidification system (2) comprises a high-pressure reaction kettle (21) and a separation tank (22) which is connected with the upper part of the high-pressure reaction kettle (21) through a material conveying pipe (210) and is used for separating oil and methanol after reaction, a second jacket heater (23) is arranged in the high-pressure reaction kettle (21), the bottom of the high-pressure reaction kettle (21) is communicated with a high-pressure reaction kettle material pipe (24), a four-way valve A (25) is connected on the high-pressure reaction kettle material pipe (24), the remaining three interfaces on the four-way valve A (25) are respectively connected with a liquid methanol conveying pipe (26) used for filling liquid methanol into the high-pressure reaction kettle (21), a raw oil conveying pipe (27) used for filling raw oil into the high-pressure reaction kettle (21), and a maintenance cleaning pipe (223) used for discharging materials during production stopping maintenance and filling into the high-pressure cleaning water reaction kettle (21), a pressure reducing valve (211), the top of the separation tank (22) is connected with a first methanol output pipe (28), the first methanol output pipe (28) is connected to a condensation recovery system, the bottom of the separation tank (22) is connected with a first grease output pipe (29), and the first grease output pipe (29) is connected to a normal-pressure deacidification system (3);

the normal-pressure deacidification system (3) comprises a normal-pressure reaction kettle (31), an alcohol separation tower (33) used for separating oil and water methanol through natural sedimentation and connected out of the normal-pressure reaction kettle (31) through a second oil material conveying pipe (32), and a pure methanol liquid storage tank (310); a third jacket heater (35) is arranged on the normal pressure reaction kettle (31), a first grease outward conveying pipe (29) for conveying grease with 5-10 fatty acid content in the normal pressure reaction kettle (31) is connected to the normal pressure reaction kettle (31), a second methanol outward conveying pipe (36) for discharging methanol gas outwards is connected to the normal pressure reaction kettle (31), the first grease outward conveying pipe (29) and the second methanol outward conveying pipe (36) are connected to the top of the normal pressure reaction kettle (31), the bottom of the normal pressure reaction kettle (31) is connected with a normal pressure reaction kettle material pipe (37), the outlet of the normal pressure reaction kettle material pipe (37) is connected with a four-way valve B (38), one interface of the four-way valve B (38) is connected with the inlet of the second oil conveying pipe (32), one interface of the four-way valve B (38) is connected with a methanol conveying pipe (39) for conveying methanol gas in the normal pressure reaction kettle (31, pure methanol liquid storage jar (310) is connected with vaporizer (312) through pure methanol liquid conveyer pipe (311), methanol delivery pipe (39) import and vaporizer (312) exit linkage, second methyl alcohol defeated outward pipe (36) insert to methanol storage jar (313), liquid methyl alcohol conveyer pipe (26) import is connected with methanol storage jar (313), the top of alcoho tower (33) is connected with second grease defeated outward pipe (315), second grease defeated outward pipe (315) insert to abandonment animal and vegetable fat production biomass fuel production system in the ester exchange system, alcoho tower (33) bottom is connected with water methyl alcohol defeated outward pipe (316), water methyl alcohol defeated outward pipe (316) insert to abandonment animal and vegetable fat production biomass fuel production system in the water methyl alcohol circulation recovery system.

2. The system for producing the fuel oil by the waste animal and vegetable oil and fat with the rapid deacidification, the low sulfur and the high yield according to the claim 1 is characterized in that a first flow meter (114) and a first pump (115) are arranged on the hydrogen peroxide conveying pipe (13), a second flow meter (116) and a second pump (117) are arranged on the first cleaning water conveying pipe (14), a third pump (118) is arranged on the waste oil conveying pipe (12), a first valve (120) is arranged on the discharging pipe (119), a second valve (121) and a fourth pump (126) are arranged on the slag oil conveying pipe (16), and a third valve (122) and a fifth pump (127) are arranged on the first oil conveying pipe (18).

3. The system for producing fuel oil by using waste animal and vegetable oil and fat to rapidly reduce acid and reduce sulfur in high yield according to claim 1, wherein one outlet of the three-phase centrifuge A (17) is connected with a secondary water washing tank (123) for carrying out secondary water washing on oil materials separated from settled slag oil materials, and the remaining two outlets are respectively connected with a slag harmless treatment system for carrying out harmless treatment on slag materials separated from settled slag oil materials and a sewage treatment system for carrying out harmless treatment on sewage separated from settled slag oil materials.

4. The system for producing fuel oil by using waste animal and vegetable oil and fat to rapidly reduce acid and reduce sulfur in high yield according to claim 1, wherein the stirrer (110) comprises a driving motor (111) arranged on the reaction kettle (11), a stirring rod (112) connected with a driving shaft of the driving motor (111) and positioned in the reaction kettle (11), and stirring blades (113) arranged on two sides of the stirring rod (112) in a staggered manner, wherein resistance reducing holes (124) are formed in the stirring blades (113), and the driving motor (111) is a forward and reverse rotating motor.

5. The system for producing fuel oil by using waste animal and vegetable oil and fat to rapidly reduce the acid and reduce the sulfur content and achieve high yield according to claim 1, wherein a spray nozzle (212) is installed at a discharge port of the feed delivery pipe (210), and the spray nozzle (212) is positioned in the middle of the inside of the separation tank (22); an eighth valve (213), a first oil pump (214) and a third flowmeter (215) are arranged on the raw oil delivery pipe (27); a ninth valve (216), a second oil pump (217) and a fourth flowmeter (218) are arranged on the liquid methanol delivery pipe (26); the first methanol output pipe (28) is provided with a fourth valve (221) and an air pump (222).

6. The system for producing fuel oil from waste animal and vegetable oil and fat with rapid deacidification and low sulfur and high yield as claimed in claim 1, wherein the overhaul cleaning pipe (223) is connected with a material drain pipe (224) and a second cleaning water conveying pipe (225), the material drain pipe (224) is connected to the material temporary storage tank (226), and the second cleaning water conveying pipe (225) is connected from the clean water tank (227).

7. The system for producing fuel oil by using waste animal and vegetable oil and fat to rapidly reduce acid and reduce sulfur and achieve high yield according to claim 6, wherein a fifth valve (228) is arranged on the maintenance cleaning pipe (223), a sixth valve (229) and a fourth oil pump (230) are arranged on the material discharging pipe (224), and a seventh valve (231) and a fifth oil pump (232) are arranged on the second cleaning water conveying pipe (225).

8. The system for producing fuel oil by rapidly reducing the acid and reducing the sulfur content in the waste animal and vegetable oil according to claim 1, wherein the second methanol export pipe (36) is provided with a condenser (314) for liquefying gaseous methanol in the second methanol export pipe (36) into liquid methanol.

9. The system for producing fuel oil by using waste animal and vegetable oil and fat to rapidly reduce the acid and reduce the sulfur content and achieve high yield according to claim 1, wherein a tenth valve (317), an eighth pump (318) and a fifth flow meter (319) are arranged on the first oil and fat delivery pipe (29); an eleventh valve (320), a second air pump (321) and a sixth flow meter (322) are arranged on the methanol delivery pipe (39), and the second air pump (321) is an air pump; a twelfth valve (323) and a third air pump (324) are arranged on the second methanol outer transmission pipe (36), and the third air pump (324) is an air pump; a thirteenth valve (325) and a ninth pump (326) are arranged on the second oil conveying pipe (32); a fourteenth valve (327) and a tenth pump (328) are arranged on the pure methanol liquid conveying pipe (311); a fifteenth valve (329) and a sixth pump (330) are arranged on the second grease output pipe (315); a sixteenth valve (331) and a seventh pump (332) are arranged on the water methanol delivery pipe (316).

10. The system for producing fuel oil by using waste animal and vegetable oil and fat to rapidly reduce acid and reduce sulfur and achieve high yield according to claim 1, wherein a seventeenth valve (333) is arranged on a material pipe (37) of the normal pressure reaction kettle, the rest interface of the four-way valve B (38) is connected with a standby pipeline (334), and an eighteenth valve (335) is arranged on the standby pipeline (334).