CN104830539A - Oil treatment system based on molecular distillation device - Google Patents
Oil treatment system based on molecular distillation device Download PDFInfo
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- CN104830539A CN104830539A CN201510245545.3A CN201510245545A CN104830539A CN 104830539 A CN104830539 A CN 104830539A CN 201510245545 A CN201510245545 A CN 201510245545A CN 104830539 A CN104830539 A CN 104830539A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/74—Recovery of fats, fatty oils, fatty acids or other fatty substances, e.g. lanolin or waxes
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Abstract
The invention relates to an oil treatment system based on a molecular distillation device. The oil treatment system comprises a molecular distiller, a reheater, a condenser, a cold well, a heavy component receiving tank, a light component receiving tank, a flow rate control system located in an oil inlet direction of the reheater and a temperature control system for controlling the temperatures of the molecular distiller and the reheater, the bottom of the reheater is communicated with an incoming oil pipeline, the top of the reheater is communicated with the upper part of the molecular distiller by an oil outlet pipeline, the lower part of the molecular distiller is communicated with the condenser, the heavy component receiving tank and the light component receiving tank respectively, and the condenser is communicated with the cold well which is sequentially communicated with a buffer tank and a vacuum unit serially. The oil treatment system can deeply purify gutter oil precisely, can acquire high-quality glycerin, has compact integral structure design and can be controlled precisely, the parameter setting operation is simple and convenient, high-quality glycerin product can be purified from gutter oil, and the oil treatment system has high production efficiency and is particularly suitable for streamlined treatment of large-scale gutter oil.
Description
Technical field
The present invention relates to oily purification techniques, particularly relate to a kind of oil treatment system based on molecular distillation apparatus.
Background technology
Sewer oil is a kind of quality extreme difference, extremely antihygienic oil product.Once edible sewer oil, it can destroy white cell and the alimentary canal mucous membrane of people, causes food poisoning, even carcinogenic serious consequence.Present China produces 7,000,000 tons, waste oil every year to 1,400 ten thousand tons, wherein heavily puts on the dining table up to 3,500,000 tons of sewer oils; Although more and more stricter to the management of sewer oil in recent years, under the ordering about of interests, still have a large amount of sewer oils to flow to catering industry, only have for sewer oil provides a production with reasonable added value could fundamentally solve the problem with process channel.
Trench main body of oil is fatty acid glycerine three fat, with the composition of natural fats and oils closely, but containing the larger impurity of a large amount of proportion; Current sewer oil reutilization technology comprises the production for the biofuel such as biofuel, hydrogen or lubrication wet goods; Due to this kind of emerging technology and immature and poor product quality and the factor such as production cost is high, sewer oil is recycled unsatisfactory.
Glycerine is that up to now, the production of glycerine is still main raw material with natural fats and oils, and wherein the natural glycerin of about 42% derives from soapmaking by-product at all very large raw material of industry requirement amount such as industry, medicine, daily use chemicals, and 58% derives from lipid acid produces.Adopt sewer oil to prepare glycerine, than employing natural fats and oils, there is obvious material cost advantage, and sewer oil recycling problem can be solved well.
Sewer oil is utilized to prepare the commercial production conditions of glycerine at present still immature, the purification of glycerine mainly come from sewer oil produce fuel after resultant product, not only cost is high, complex process, be difficult to realize industrialization, such as, and the glycerine produced also is difficult to the feed quality requirements meeting association area, the purification process of the by product raw glycerine of a kind of Preparation of biodiesel from waste oils disclosed in Chinese patent ZL201310720341.1.The current subject matter from sewer oil Purifing of Glycerol technology is the selection of production unit, device control, processing parameter and production quality control etc.
Summary of the invention
The object of this invention is to provide a kind of oil treatment system based on molecular distillation apparatus, it is high that it has auto-control degree, the advantage that product separation efficiency is high and reliable and stable.
The present invention is achieved like this, a kind of oil treatment system based on molecular distillation apparatus, it comprises molecular still, it is characterized in that, it also comprises reheater, condenser, Leng Jing, heavy constituent receiving tank, light constituent receiving tank and the flow control system be positioned on reheater oil-feed direction and for molecular still and the temperature controlled temperature control system of reheater;
Be communicated with to come oil line bottom described reheater, top is communicated with molecular still top by outlet line; The bottom of molecular still is communicated in condenser, heavy constituent receiving tank and light constituent receiving tank respectively, condenser is communicated with cold well, cold well is communicated with vacuum pump set with surge tank again successively, and light constituent receiving tank is connected with cold gas well gas with heavy constituent receiving tank, condenser again respectively by pipeline;
The bottom of described heavy constituent receiving tank and light constituent receiving tank is equipped with electric flow control valve.
Described flow control system comprises electric flow control valve, flow director and spinner-type flowmeter, between spinner-type flowmeter is connected in bottom electric flow control valve and reheater, be electrically connected with flow director between spinner-type flowmeter and electric flow control valve, the two ends of described spinner-type flowmeter respectively after series connected valve again with a valve in parallel.
Described temperature control system is under the control of temperature controller, thermal oil from thermal oil inlet pipe is pumped into reheater and molecular still respectively through four-way valve, the flow of thermal oil is through valve regulated, and the thermal oil of discharging from reheater and molecular still enters into thermal oil through four-way valve again and goes out pipe.
Preferably: described molecular still bottom also goes out pipe with recirculated water inlet pipe and recirculated water respectively by pipeline and is communicated with, cold aboveground portion also goes out to manage with refrigerated water by pipeline and is communicated with refrigerated water inlet pipe.
Described reheater comprises discharge port, temperature-measuring port, tube sheet, venting port, thermal oil outlet, traverse baffle, pull bar, spacing tube, heat transfer tube, heat conductive oil inlet, discharging hole and opening for feed, discharge port and temperature-measuring port are communicated with the top at reheater respectively, and opening for feed is communicated with in the bottom of reheater;
The upper and lower of reheater is respectively equipped with a tube sheet, and two tube sheets and reheater inwall form heat exchange chamber, and the top and bottom of two parallel heat transfer tubes are each passed through tube sheet and are communicated with opening for feed with discharge port; The venting port and the thermal oil outlet that are positioned at reheater top are communicated in heat exchange chamber respectively, and the heat conductive oil inlet and the discharging hole that are positioned at reheater bottom are also communicated in heat exchange chamber respectively;
Heat exchange chamber is divided into several baffling chambeies be communicated with continuously by several traverse baffles, pull bar and spacing tube; Wherein, traverse baffle is staggered along heat exchange chamber vertical direction level, and traverse baffle is by coupled spacing tube adjustment height, and spacing tube is connected to the lower end of pull bar, and the upper end of pull bar is fixed on bottom the tube sheet on reheater top.
Preferably: the described baffling chamber that several are communicated with continuously forms the continuous passage of S type or Z-type jointly.
Described molecular still comprises the power system, end socket, heating cylinder, receptor and the bobbin carriage that are fixedly linked successively from the top down, end socket is provided with the opening for feed be communicated with heating cylinder, the coiling of heating cylinder periphery has some heating coils, the upper end of described heating coil is thermal oil outlet, and lower end is heat conductive oil inlet; Receptor both sides are communicated with heavy constituent outlet, secondary steam outlet and light fraction outlet respectively, and heavy constituent outlet is communicated with heavy constituent receiving tank, light constituent receiving tank respectively with light fraction outlet; Bobbin carriage is communicated with condensation-water drain and water of condensation import respectively, and condensation-water drain and water of condensation import respectively communication loop water go out pipe and recirculated water inlet pipe.
The top of described condenser and bottom are communicated with circulating water outlet and circulating water intake respectively, the central enclosure of condenser forms condensing chamber with the baffle plate laying respectively at case top and bottom, and the heat transfer tube two ends being positioned at condensing chamber are communicated with circulating water intake with circulating water outlet respectively;
Condensing chamber is divided into several baffling chambeies be communicated with continuously by several pull bars, traverse baffle and spacing tube; Wherein, traverse baffle is staggered along heat exchange chamber vertical direction level, and traverse baffle is by coupled spacing tube adjustment height, and spacing tube is connected to the lower end of pull bar, and the upper end of pull bar is fixed on bottom the baffle plate of case top; Vapor phase exit is positioned at the top of housing, and vapor phase exit is communicated with between condensing chamber and cold well; Vapour phase import and material liquid outlet are arranged on the bottom of housing from the top down successively, its two ends of vapour phase import respectively with the secondary steam outlet in condensing chamber and molecular still; Material liquid outlet is connected with Leng Jing with light constituent receiving tank by pipeline.
Described cold well comprises the bobbin carriage, refrigeration chamber and the end socket that are fixedly connected sequentially from the top down, described bobbin carriage and refrigeration chamber and all separated by tube sheet between ellipsoidal head and refrigeration chamber; Described bobbin carriage inner chamber is divided into two independently chambers by dividing plate, and two chamber roof are communicated with chilled water inlet and chilled water outlet respectively, and chilled water inlet and chilled water outlet are communicated with refrigerated water inlet pipe respectively and refrigerated water goes out pipe;
Be provided with two heat transfer tubes in refrigeration chamber, the upper end of one of them heat transfer tube and bobbin carriage chamber, the upper end of another heat transfer tube and another chamber of bobbin carriage, and the lower end of heat transfer tube is connected through after the tube sheet of bottom; Refrigeration chamber is divided into several baffling chambeies be communicated with continuously by several pull bars, distance rod and traverse baffle, wherein, traverse baffle is staggered along refrigeration chamber vertical direction level, traverse baffle is by coupled distance rod adjustment height, distance rod is connected to the lower end of pull bar, and the upper end of pull bar is fixed on the tube sheet of top;
Refrigeration chamber top is provided with the vapour outlet be communicated with surge tank, both sides, refrigeration chamber bottom are communicated with material steam entrance and leakage fluid dram respectively, material steam entrance is communicated with the vapor phase exit in condenser by pipeline, and leakage fluid dram is communicated with light constituent receiving tank again after being communicated with the material liquid outlet of condenser by pipeline; The bottom of described end socket is also provided with discharging hole.
Beneficial effect of the present invention is: the present invention be a kind of can from sewer oil the assembly line equipment of automatization Purifing of Glycerol, especially can realize the process of sewer oil middle rank, sub-argument can go out the equipment of the glycerine of high-quality, it is compact that it has overall construction design, control precisely, parameter setting is simple and convenient; Can to purify from sewer oil high-quality glycerol product, and it is high to have production efficiency, is applicable to very much the streamlined process to sewer oil in enormous quantities.
Accompanying drawing explanation
Fig. 1 is the structural representation of an embodiment of the present invention.
Fig. 2 is the structural representation of reheater of the present invention.
Fig. 3 is the structural representation of molecular still of the present invention.
Fig. 4 is the structural representation of condenser of the present invention.
Fig. 5 is the structural representation of the cold well of the present invention.
Embodiment
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described further.
As shown in Figure 1, one's duty invention is achieved like this, oil treatment system based on molecular distillation apparatus comprises molecular still 3, it is characterized in that, it also comprises reheater 2, condenser 4, cold well 5, heavy constituent receiving tank 6, light constituent receiving tank 7 and the flow control system 1 be positioned on reheater 2 oil-feed direction and for molecular still 3 and the temperature controlled temperature control system 10 of reheater 2;
Be communicated with to come oil line bottom described reheater 2, top is communicated with molecular still 3 top by outlet line; The bottom of molecular still 3 is communicated in condenser 4, heavy constituent receiving tank 6 and light constituent receiving tank 7 respectively, condenser 4 is communicated with cold well 5, cold well 5 is communicated with vacuum pump set 9 with surge tank 8 again successively, and light constituent receiving tank 7 is communicated with cold well 5 gas phase with heavy constituent receiving tank 6, condenser 4 again respectively by pipeline; The bottom of described heavy constituent receiving tank 6 and light constituent receiving tank 7 is equipped with electric flow control valve.
Its basic functional principle is, under the control of temperature control system 10 and flow control system 1, pending oil product is through reheater 2, separation is distilled at molecular still 3, the aperture of the molecular film that molecular still 3 adopts is set, accurately oil product can be separated into heavy constituent oil product and glycerine, and be stored in heavy constituent receiving tank 6 and light constituent receiving tank 7 respectively, whole treating processes adjusts operating pressure by surge tank 8 and coupled vacuum pump set 9; Glycerine in pretreated sewer oil can be purified by this system, and not only control simple and convenient, purification efficiency and quality also greatly improve, and achieve the suitability for industrialized production of sewer oil process.
The bottom of described heavy constituent receiving tank 6 and light constituent receiving tank 7 is equipped with electric flow control valve; According to output demand, electric flow control valve can be utilized to adjust the quantum of output of glycerol product, and controls the flow of secondary oil product raw material in heavy constituent receiving tank 5.
Described flow control system 1 comprises electric flow control valve, flow director and spinner-type flowmeter, between spinner-type flowmeter is connected in bottom electric flow control valve and reheater 2, be electrically connected with flow director between spinner-type flowmeter and electric flow control valve, the two ends of described spinner-type flowmeter respectively after series connected valve again with a valve in parallel.Utilize flow control system 1, rationally can arrange the supply flow rate of stock oil, it and temperature control system 10 are worked in coordination with, and make pending oil product distilation under the environment of setting, level of automation greatly improves.
Temperature control system 10 is under the control of temperature controller, thermal oil from thermal oil inlet pipe is pumped into reheater 2 and molecular still 3 respectively through four-way valve, the flow of thermal oil is through valve regulated, and the thermal oil of discharging from reheater 2 and molecular still 3 enters into thermal oil through four-way valve again and goes out pipe.
As shown in Figure 2, described reheater 2 comprises discharge port 201, temperature-measuring port 202, tube sheet 203, venting port 204, thermal oil outlet 205, traverse baffle 206, pull bar 207, spacing tube 208, heat transfer tube 209, heat conductive oil inlet 210, discharging hole 211 and opening for feed 212, discharge port 201 and temperature-measuring port 202 are communicated with at the top of reheater 2 respectively, and opening for feed 212 is communicated with the bottom at reheater 2; The upper and lower of reheater 2 is respectively equipped with tube sheet 203, two tube sheet 203 and forms heat exchange chamber with reheater 2 inwall, and the top and bottom of two parallel heat transfer tubes 209 are each passed through tube sheet 203 and are communicated with opening for feed 212 with discharge port 201; The venting port 204 and the thermal oil outlet 205 that are positioned at reheater 2 top are communicated in heat exchange chamber respectively, and the heat conductive oil inlet 210 and the discharging hole 211 that are positioned at reheater 2 bottom are also communicated in heat exchange chamber respectively; Heat conductive oil inlet 210 directly can carry out hydraulic fluid port with the four-way valve in temperature control system 10 and be communicated with;
Heat exchange chamber is divided into several baffling chambeies be communicated with continuously by several traverse baffles 206, pull bar 207 and spacing tube 208; Wherein, traverse baffle 206 is staggered along heat exchange chamber vertical direction level, traverse baffle 206 adjusts height by coupled spacing tube 208, and spacing tube 208 is connected to the lower end of pull bar 207, and the upper end of pull bar 207 is fixed on bottom the tube sheet 203 on reheater 2 top.The described baffling chamber that several are communicated with continuously forms the continuous passage of S type or Z-type jointly.
Pending oil product from bottom to top, heated by heat exchange chamber through opening for feed 212, heat transfer tube 209 and discharge port 201 successively, in heat exchange chamber, the restriction of several baffling chambeies is flowed in heat transfer tube 209 periphery around/fold back from bottom to top from the thermal oil of heat conductive oil inlet 210, substantially increase the efficiency of heat exchange like this, ensure stock oil thermally equivalent, and more optimal design is: several baffling chambeies be communicated with continuously form the continuous passage of S type or Z-type jointly, can improve the heat exchange efficiency of heat exchange chamber further.Utilize the temperature sensor of temperature-measuring port 202, in time the temperature of heat exchange chamber is passed to temperature control system 10, utilize temperature control system 10 and flow control system 1 to adjust the temperature that stock oil enters molecular still 3, for evaporation purification is prepared.
Institute as shown in Figure 3, molecular still 3 comprises the power system 312, end socket 313, heating cylinder 308, receptor 304 and the bobbin carriage 302 that are fixedly linked successively from the top down, end socket 313 is provided with the opening for feed 311 be communicated with heating cylinder 308, the coiling of heating cylinder 308 periphery has some heating coils 309, the upper end of described heating coil 309 is thermal oil outlet 310, and lower end is heat conductive oil inlet 307;
Receptor 304 both sides are communicated with heavy constituent outlet 305, secondary steam outlet 306 and light fraction outlet 314 respectively, and heavy constituent outlet 305 is communicated with heavy constituent receiving tank 6, light constituent receiving tank 7 respectively with light fraction outlet 314; Bobbin carriage 302 is communicated with condensation-water drain 301 and water of condensation import 303 respectively, condensation-water drain 301 and water of condensation import 303 respectively communication loop water go out pipe and recirculated water inlet pipe, and namely described molecular still 3 bottom also goes out pipe with recirculated water inlet pipe and recirculated water respectively by pipeline and is communicated with.
The heat conductive oil inlet 307 of molecular still 3 directly carrys out hydraulic fluid port with the four-way valve in temperature control system 10 and is communicated with, oil product is after reheater 2 heats, entered by opening for feed 311, successively through end socket 313, heating cylinder 308, receptor 304 and bobbin carriage 302, under the heating of heating cylinder 308 periphery hot coil 309, realize fractionation by distillation and purify; The aperture of conservative control Heating temperature and molecular distillation, the fine separation that can realize oil product is purified, wherein light constituent is discharged from light fraction outlet 314 and secondary steam outlet 306 respectively with liquid and gaseous state, liquid light constituent directly enters light constituent receiving tank 7, and gaseous light component needs just can enter in light constituent receiving tank 7 through condenser 4 and the further condensation of cold well 5; Heavy constituent directly enters heavy constituent receiving tank 6 by heavy constituent outlet 305; The main purified product of light constituent is glycerol product; Heavy constituent then can be further used as the raw material of purification.
As shown in Figure 4, the top of condenser 4 and bottom are communicated with circulating water outlet 401 and circulating water intake 409 respectively, the central enclosure of condenser 4 forms condensing chamber with the baffle plate 402 laying respectively at case top and bottom, and heat transfer tube 410 two ends being positioned at condensing chamber are communicated with circulating water intake 409 with circulating water outlet 401 respectively;
Condensing chamber is divided into several baffling chambeies be communicated with continuously by several pull bars 404, traverse baffle 405 and spacing tube 406; Wherein, traverse baffle 405 is staggered along heat exchange chamber vertical direction level, and traverse baffle 405 adjusts height by coupled spacing tube 406, and spacing tube 406 is connected to the lower end of pull bar 404, and the upper end of pull bar 404 is fixed on bottom the baffle plate 402 of case top;
Vapor phase exit 407 is positioned at the top of housing, and vapor phase exit 407 is communicated with between condensing chamber and cold well 5; Vapour phase import 403 and material liquid outlet 408 are arranged on the bottom of housing from the top down successively, and its two ends of vapour phase import 403 export 306 with condensing chamber and the secondary steam in molecular still 3 respectively and are communicated with; Material liquid outlet 408 is connected with cold well 5 with light constituent receiving tank 7 by pipeline.
The principle of work of condenser 4 is: the gaseous light component entered from vapour phase import 403 along baffling chamber around or baffling in heat transfer tube 410 periphery, gaseous light component is condensed into liquid state, light constituent receiving tank 6 is entered through material liquid outlet 408, the part gaseous light component be not condensed then enters cold well 5 through vapor phase exit 407, further condensation light constituent; If condensing chamber pressure is excessive, then regulate pressure through surge tank 8 and coupled vacuum pump set 9.
In actual production, need set temperature sensor between secondary steam outlet 306 and vapour phase import 403, and condenser 4, heavy constituent receiving tank 6 and light constituent receiving tank 7 all need set temperature sensor, utilize temperature control system 10 can reasonable adjusting condenser 4 condensing temperature and enter the temperature of oil product product in heavy constituent receiving tank 6 and light constituent receiving tank 7, optimized production process.
As shown in Figure 5, cold well 5 comprises bobbin carriage 503, refrigeration chamber and the end socket 514 be fixedly connected sequentially from the top down, described bobbin carriage 503 and refrigeration chamber and all separated by tube sheet 513 between ellipsoidal head 514 and refrigeration chamber; Described bobbin carriage 503 inner chamber is divided into two independently chambers by dividing plate 504, two chamber roof are communicated with chilled water inlet 501 and chilled water outlet 502 respectively, chilled water inlet 501 and chilled water outlet 502 are communicated with refrigerated water inlet pipe and refrigerated water respectively and go out pipe, and namely cold well 5 top goes out to manage with refrigerated water by pipeline and is communicated with refrigerated water inlet pipe;
Two heat transfer tubes 509 are provided with in refrigeration chamber, the upper end of one of them heat transfer tube 509 and a chamber of bobbin carriage 503, the upper end of another heat transfer tube 509 and another chamber of bobbin carriage 503, and the lower end of heat transfer tube 509 is connected through after the tube sheet 513 of bottom; Refrigeration chamber is divided into several baffling chambeies be communicated with continuously by several pull bars 506, distance rod 508 and traverse baffle 507, wherein, traverse baffle 507 is staggered along refrigeration chamber vertical direction level, traverse baffle 507 adjusts height by coupled distance rod 508, distance rod 508 is connected to the lower end of pull bar 506, and the upper end of pull bar 506 is fixed on the tube sheet 513 of top;
Refrigeration chamber top is provided with the vapour outlet 505 be communicated with surge tank 8, both sides, refrigeration chamber bottom are communicated with material steam entrance 510 and leakage fluid dram 511 respectively, material steam entrance 510 is communicated with the vapor phase exit 407 in condenser 4 by pipeline, and leakage fluid dram 511 is communicated with light constituent receiving tank 7 again after being communicated with the material liquid outlet 408 of condenser 4 by pipeline; The bottom of described end socket 514 is also provided with discharging hole 512
Cold well 5 proposes further to realize light constituent and arranges, and from the light constituent steam of material steam entrance 510 through refrigeration chamber, back and forth flows at heat transfer tube 509 from bottom to top along traverse baffle 507; Because temperature is lower, gaseous light component can be condensed into liquid light constituent, enter in light constituent receiving tank 7, and other gases being difficult to condensation is cushioned by surge tank 8 through vapour outlet 505 through leakage fluid dram 511, discharges finally by vacuum pump set 9.
Claims (9)
1. the oil treatment system based on molecular distillation apparatus, it comprises molecular still (3), it is characterized in that, it also comprises reheater (2), condenser (4), cold well (5), heavy constituent receiving tank (6), light constituent receiving tank (7) and the flow control system (1) be positioned on reheater (2) oil-feed direction and for molecular still (3) and reheater (2) temperature controlled temperature control system (10);
Described reheater (2) bottom is communicated with to come oil line, and top is communicated with molecular still (3) top by outlet line; The bottom of molecular still (3) is communicated in condenser (4), heavy constituent receiving tank (6) and light constituent receiving tank (7) respectively, condenser (4) is communicated with cold well (5), cold well (5) is communicated with vacuum pump set (9) with surge tank (8) again successively
Light constituent receiving tank (7) is communicated with cold well (5) gas phase with heavy constituent receiving tank (6), condenser (4) again respectively by pipeline;
The bottom of described heavy constituent receiving tank (6) and light constituent receiving tank (7) is equipped with electric flow control valve.
2. as claimed in claim 1 based on the oil treatment system of molecular distillation apparatus, described flow control system (1) comprises electric flow control valve, flow director and spinner-type flowmeter, spinner-type flowmeter is connected between electric flow control valve and reheater (2) bottom, be electrically connected with flow director between spinner-type flowmeter and electric flow control valve, the two ends of described spinner-type flowmeter respectively after series connected valve again with a valve in parallel.
3. as claimed in claim 1 or 2 based on the oil treatment system of molecular distillation apparatus, described temperature control system (10) is under the control of temperature controller, thermal oil from thermal oil inlet pipe is pumped into reheater (2) and molecular still (3) respectively through four-way valve, the flow of thermal oil is through valve regulated, and the thermal oil of discharging from reheater (2) and molecular still (3) enters into thermal oil through four-way valve again and goes out pipe.
4. as claimed in claim 3 based on the oil treatment system of molecular distillation apparatus, described molecular still (3) bottom also goes out pipe with recirculated water inlet pipe and recirculated water respectively by pipeline and is communicated with, and cold well (5) top also goes out to manage with refrigerated water by pipeline and is communicated with refrigerated water inlet pipe.
5. as claimed in claim 4 based on the oil treatment system of molecular distillation apparatus, described reheater (2) comprises discharge port (201), temperature-measuring port (202), tube sheet (203), venting port (204), thermal oil outlet (205), traverse baffle (206), pull bar (207), spacing tube (208), heat transfer tube (209), heat conductive oil inlet (210), discharging hole (211) and opening for feed (212), discharge port (201) is communicated with the top in reheater (2) respectively with temperature-measuring port (202), opening for feed (212) is communicated with the bottom in reheater (2),
The upper and lower of reheater (2) is respectively equipped with a tube sheet (203), two tube sheets (203) and reheater (2) inwall form heat exchange chamber, and the top and bottom of two parallel heat transfer tubes (209) are each passed through tube sheet (203) and are communicated with opening for feed (212) with discharge port (201);
The venting port (204) and thermal oil outlet (205) that are positioned at reheater (2) top are communicated in heat exchange chamber respectively, and the heat conductive oil inlet (210) and the discharging hole (211) that are positioned at reheater (2) bottom are also communicated in heat exchange chamber respectively;
Heat exchange chamber is divided into several baffling chambeies be communicated with continuously by several traverse baffles (206), pull bar (207) and spacing tube (208); Wherein, traverse baffle (206) is staggered along heat exchange chamber vertical direction level, traverse baffle (206) is by coupled spacing tube (208) adjustment height, spacing tube (208) is connected to the lower end of pull bar (207), and the upper end of pull bar (207) is fixed on tube sheet (203) bottom on reheater (2) top.
6. as claimed in claim 5 based on the oil treatment system of molecular distillation apparatus, it is characterized in that, the described baffling chamber that several are communicated with continuously forms the continuous passage of S type or Z-type jointly.
7. the oil treatment system based on molecular distillation apparatus as described in claim 5 or 6, it is characterized in that, described molecular still (3) comprises the power system (312) be fixedly linked successively from the top down, end socket (313), heating cylinder (308), receptor (304) and bobbin carriage (302), end socket (313) is provided with the opening for feed (311) be communicated with heating cylinder (308), the coiling of heating cylinder (308) periphery has some heating coils (309), the upper end of described heating coil (309) is thermal oil outlet (310), lower end is heat conductive oil inlet (307),
Receptor (304) both sides are communicated with heavy constituent outlet (305), secondary steam outlet (306) and light fraction outlet (314) respectively, and heavy constituent outlet (305) is communicated with heavy constituent receiving tank (6), light constituent receiving tank (7) respectively with light fraction outlet (314); Bobbin carriage (302) is communicated with condensation-water drain (301) and water of condensation import (303) respectively, and condensation-water drain (301) and water of condensation import (303) respectively communication loop water inlet pipe and recirculated water go out pipe.
8. as claimed in claim 7 based on the oil treatment system of molecular distillation apparatus, it is characterized in that, the top of described condenser (4) and bottom are communicated with circulating water outlet (401) and circulating water intake (409) respectively, the central enclosure of condenser (4) forms condensing chamber with the baffle plate (402) laying respectively at case top and bottom, and heat transfer tube (410) two ends being positioned at condensing chamber are communicated with circulating water intake (409) with circulating water outlet (401) respectively;
Condensing chamber is divided into several baffling chambeies be communicated with continuously by several pull bars (404), traverse baffle (405) and spacing tube (406); Wherein, traverse baffle (405) is staggered along heat exchange chamber vertical direction level, traverse baffle (405) is by coupled spacing tube (406) adjustment height, spacing tube (406) is connected to the lower end of pull bar (404), and the upper end of pull bar (404) is fixed on baffle plate (402) bottom of case top;
Vapor phase exit (407) is positioned at the top of housing, and vapor phase exit (407) is communicated with between condensing chamber and Leng Jing (5);
Vapour phase import (403) and material liquid outlet (408) are arranged on the bottom of housing from the top down successively, and vapour phase import (403) its two ends export (306) with condensing chamber with the secondary steam in molecular still (3) respectively and are communicated with; Material liquid outlet (408) is connected with cold well (5) with light constituent receiving tank (7) by pipeline.
9. as claimed in claim 8 based on the oil treatment system of molecular distillation apparatus, described cold well (5) comprises the bobbin carriage (503), refrigeration chamber and the end socket (514) that are fixedly connected sequentially from the top down, described bobbin carriage (503) and refrigeration chamber and all separated by tube sheet (513) between ellipsoidal head (514) and refrigeration chamber;
Described bobbin carriage (503) inner chamber is divided into two independently chambers by dividing plate (504), and two chamber roof are communicated with chilled water inlet (501) and chilled water outlet (502) respectively; Chilled water inlet (501) and chilled water outlet (502) are communicated with refrigerated water inlet pipe respectively and refrigerated water goes out pipe;
Two heat transfer tubes (509) are provided with in refrigeration chamber, the upper end of one of them heat transfer tube (509) and a chamber of bobbin carriage (503), the upper end of another heat transfer tube (509) and another chamber of bobbin carriage (503), and the lower end of heat transfer tube (509) is connected through after the tube sheet (513) of bottom; Refrigeration chamber is divided into several baffling chambeies be communicated with continuously by several pull bars (506), distance rod (508) and traverse baffle (507), wherein, traverse baffle (507) is staggered along refrigeration chamber vertical direction level, traverse baffle (507) is by coupled distance rod (508) adjustment height, distance rod (508) is connected to the lower end of pull bar (506), and the upper end of pull bar (506) is fixed on the tube sheet (513) of top;
Refrigeration chamber top is provided with the vapour outlet (505) be communicated with surge tank (8), both sides, refrigeration chamber bottom are communicated with material steam entrance (510) and leakage fluid dram (511) respectively, material steam entrance (510) is communicated with the vapor phase exit (407) in condenser (4) by pipeline, and leakage fluid dram (511) is communicated with light constituent receiving tank (7) again after being communicated with the material liquid outlet (408) of condenser (4) by pipeline;
The bottom of described end socket (514) is also provided with discharging hole (512).
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| Application Number | Priority Date | Filing Date | Title |
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| CN201510245545.3A CN104830539A (en) | 2015-05-14 | 2015-05-14 | Oil treatment system based on molecular distillation device |
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| CN201510245545.3A CN104830539A (en) | 2015-05-14 | 2015-05-14 | Oil treatment system based on molecular distillation device |
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| CN104830539A true CN104830539A (en) | 2015-08-12 |
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Effective date of registration: 20150924 Address after: Shijing Street crow village Xinchang Baiyun District of Guangzhou City, Guangdong Province, No. 1 by 510000 Applicant after: Hairma Chemicals (GZ) Ltd. Address before: 226009 No. 1, Yongshun Road, Nantong economic and Technological Development Zone, Jiangsu, China Applicant before: Nantong Hirma Grease Oil Co., Ltd. Applicant before: Hairma Chemicals (GZ) Ltd. |
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