CN106675415B - Rosin production system of processing - Google Patents
Rosin production system of processing Download PDFInfo
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- CN106675415B CN106675415B CN201611200232.7A CN201611200232A CN106675415B CN 106675415 B CN106675415 B CN 106675415B CN 201611200232 A CN201611200232 A CN 201611200232A CN 106675415 B CN106675415 B CN 106675415B
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- RSWGJHLUYNHPMX-UHFFFAOYSA-N Abietic-Saeure Natural products C12CCC(C(C)C)=CC2=CCC2C1(C)CCCC2(C)C(O)=O RSWGJHLUYNHPMX-UHFFFAOYSA-N 0.000 title claims abstract description 66
- KHPCPRHQVVSZAH-HUOMCSJISA-N Rosin Natural products O(C/C=C/c1ccccc1)[C@H]1[C@H](O)[C@@H](O)[C@@H](O)[C@@H](CO)O1 KHPCPRHQVVSZAH-HUOMCSJISA-N 0.000 title claims abstract description 66
- KHPCPRHQVVSZAH-UHFFFAOYSA-N trans-cinnamyl beta-D-glucopyranoside Natural products OC1C(O)C(O)C(CO)OC1OCC=CC1=CC=CC=C1 KHPCPRHQVVSZAH-UHFFFAOYSA-N 0.000 title claims abstract description 66
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 23
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 71
- 239000001739 pinus spp. Substances 0.000 claims abstract description 39
- 229940036248 turpentine Drugs 0.000 claims abstract description 39
- 241000779819 Syncarpia glomulifera Species 0.000 claims abstract description 37
- 238000010438 heat treatment Methods 0.000 claims abstract description 27
- 238000003860 storage Methods 0.000 claims abstract description 22
- 230000007704 transition Effects 0.000 claims abstract description 14
- 239000002893 slag Substances 0.000 claims abstract description 11
- 239000007788 liquid Substances 0.000 claims description 39
- 238000004821 distillation Methods 0.000 claims description 28
- 239000012535 impurity Substances 0.000 claims description 27
- 239000002994 raw material Substances 0.000 claims description 23
- 238000002156 mixing Methods 0.000 claims description 21
- 238000007599 discharging Methods 0.000 claims description 15
- 239000004519 grease Substances 0.000 claims description 13
- 238000001816 cooling Methods 0.000 claims description 10
- 238000004062 sedimentation Methods 0.000 claims description 9
- 239000001293 FEMA 3089 Substances 0.000 claims description 2
- 235000017166 Bambusa arundinacea Nutrition 0.000 claims 4
- 235000017491 Bambusa tulda Nutrition 0.000 claims 4
- 241001330002 Bambuseae Species 0.000 claims 4
- 235000015334 Phyllostachys viridis Nutrition 0.000 claims 4
- 239000011425 bamboo Substances 0.000 claims 4
- 230000000694 effects Effects 0.000 abstract description 8
- 238000005265 energy consumption Methods 0.000 abstract description 7
- 230000008901 benefit Effects 0.000 abstract description 4
- 238000001556 precipitation Methods 0.000 abstract description 4
- 238000005352 clarification Methods 0.000 description 11
- 238000004090 dissolution Methods 0.000 description 10
- 150000002632 lipids Chemical class 0.000 description 8
- 238000000034 method Methods 0.000 description 8
- 239000011229 interlayer Substances 0.000 description 5
- 238000010586 diagram Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000003825 pressing Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 235000008331 Pinus X rigitaeda Nutrition 0.000 description 1
- 235000011613 Pinus brutia Nutrition 0.000 description 1
- 241000018646 Pinus brutia Species 0.000 description 1
- RSWGJHLUYNHPMX-ONCXSQPRSA-N abietic acid Chemical compound C([C@@H]12)CC(C(C)C)=CC1=CC[C@@H]1[C@]2(C)CCC[C@@]1(C)C(O)=O RSWGJHLUYNHPMX-ONCXSQPRSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000010410 layer Substances 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 238000010309 melting process Methods 0.000 description 1
- 229930014626 natural product Natural products 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 238000004382 potting Methods 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
- C09F—NATURAL RESINS; FRENCH POLISH; DRYING-OILS; OIL DRYING AGENTS, i.e. SICCATIVES; TURPENTINE
- C09F1/00—Obtaining purification, or chemical modification of natural resins, e.g. oleo-resins
- C09F1/02—Purification
-
- C—CHEMISTRY; METALLURGY
- C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
- C09F—NATURAL RESINS; FRENCH POLISH; DRYING-OILS; OIL DRYING AGENTS, i.e. SICCATIVES; TURPENTINE
- C09F1/00—Obtaining purification, or chemical modification of natural resins, e.g. oleo-resins
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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Abstract
The invention belongs to the field of rosin production and processing equipment, and particularly relates to a rosin production and processing system which comprises a dissolving device, a solar water heating device, a steam generating device, a hot oil device, a slag hopper, a lifting device, an oil volatilization device, a high-level cylinder, a clarifying tank, an overflow pipe, a precipitation outlet, a transition cylinder, a preheating pot, a distilling tower, a rosin storage tank, a spiral heat exchanger, an oil-water separator and a turpentine storage tank. The rosin production and processing system provided by the invention has the advantages of fast temperature rise, low energy consumption, high production efficiency and good effect, realizes comprehensive improvement in the traditional processing system, and achieves better economic benefit.
Description
Technical Field
The invention belongs to the field of rosin production and processing equipment, and particularly relates to a rosin production and processing system.
Background
Rosin is a volatile material in rosin processing and is a solid product left after steam evaporation. Rosin is a natural product secreted from pine tree resins, which is insoluble in water, but soluble in various organic solvents. The rosin production and processing mainly uses a batch steam method, which mainly comprises three procedures of melting, clarifying and distilling.
The melting process mainly comprises mixing Colophonium, turpentine and water at a certain ratio, and heating and dissolving in a dissolving kettle to remove most of impurities. The traditional dissolving device has the advantages of slow temperature rise, high energy consumption, poor dissolving efficiency and poor effect, and after the dissolving is finished, a large amount of turpentine is attached to impurities, so that the impurities are directly discharged to cause waste, and the production cost is increased.
The clarifying process mainly comprises the step of pressing the dissolved rosin into a clarifying tank from a dissolving kettle by utilizing steam pressure to deposit, so as to remove impurities and partial water in the rosin. Traditional clarifier sets up for horizontal arrangement, connects through the overflow pipe between two adjacent clarifiers, and the overflow pipe sets up in the clarifier upper end. When rosin is introduced into the clarifying tank, the flow rate of the rosin is large, so that a large impact force is caused on the rosin in the clarifying tank, and the sedimentation effect is poor, so that more clarifying tanks are required to be horizontally arranged, and the current number of clarifying tanks is generally 6-8, the equipment cost is increased, and the sedimentation efficiency is reduced. And more clarifying tanks are horizontally arranged, the rosin temperature in the latter clarifying tank is lower, and solidification phenomenon can occur. After clarification, hot water is required to be introduced into the clarification tank to remove the fat liquid in the clarification tank, all the fat liquid in the clarification tank is required to be discharged at present, all the clarification tank is required to be filled with hot water, and the hot water consumption is large.
The distillation process mainly removes turpentine oil and water in the removed rosin to obtain finished rosin. The traditional distillation procedure is to directly introduce the rosin after impurity removal into a distillation tower, the temperature of the rosin is about 90 ℃ when the rosin is introduced, and the rosin can be fully separated only when the temperature of the rosin reaches 180-200 ℃ during distillation, and the rosin is directly heated in the distillation tower for a long time, so that the distillation efficiency is not high.
Disclosure of Invention
In order to solve the problems of the prior art, the invention provides the rosin production and processing system which has the advantages of quick temperature rise, low energy consumption, high production efficiency and good effect.
The technical proposal is as follows:
a rosin production and processing system comprises a dissolving device, a solar water heating device, a steam generating device, a hot oil device, a slag hopper, a lifting device, an oil volatilization device, a high-level cylinder, a clarifying tank, an overflow pipe, a precipitation outlet, a transition cylinder, a preheating pot, a distillation tower, a rosin storage tank, a spiral heat exchanger, an oil-water separator and a turpentine storage tank;
the dissolving device comprises an outer tank body, an inner tank body, an interlayer, a hot oil coil pipe, a impurity removing grid, an impurity removing valve, a propeller, a motor, a steam inlet, a hot water inlet, a mixed raw material inlet pipe, a steam outlet pipe, a steam inlet pipe, a fat liquor discharge pipe, a mixing box and a cooling device, wherein the inner tank body is arranged in the outer tank body;
the hot water inlet is connected with a solar water heating device;
the steam inlet and the steam inlet pipe are connected with a steam generating device, and the steam generating device is connected with a solar water heating device;
the two ends of the hot oil coil pipe are connected with a hot oil device, an annular coil pipe is arranged around the hot oil device, and the two ends of the annular coil pipe are connected with a solar water heating device;
the device comprises a mixing box, a spiral feeder, a solar hot water pipe, a turpentine inlet pipe and a return pipe, wherein the mixing box is arranged at the upper end of the mixing raw material inlet pipe, the spiral feeder is arranged in the mixing box, and a raw material inlet, the solar hot water pipe, the turpentine inlet pipe and the return pipe are arranged above the mixing box;
the steam outlet pipe is provided with a cooling device which is connected with a return pipe;
the impurity removing valve is externally provided with a slag hopper which is connected to the lifting device, an oil volatilization device is arranged below the lifting device, and the upper end of the oil volatilization device is connected with a turpentine inlet pipe through a pipeline;
the grease liquid discharge pipe upper end is connected with a high-level cylinder, the high-level cylinder lower extreme is connected with a clarifying tank through a pipeline, the clarifying tank is horizontally arranged in parallel and is connected with a plurality of clarifying tanks through overflow pipes, the lower end of each clarifying tank is provided with a sedimentation outlet, a serpentine coil is arranged in each clarifying tank, two ends of each serpentine coil are connected with a steam generating device, each clarifying tank is connected with a transition cylinder, the lower end of each transition cylinder is connected with a preheating pot through a pipeline, the lower end of each preheating pot is connected with a distillation tower through a pipeline, the lower end of each distillation tower is connected with a rosin storage tank through a pipeline, the upper ends of each preheating pot and each distillation tower are connected with a spiral heat exchanger through a pipeline, each spiral heat exchanger is connected with an oil-water separator, each oil-water separator is connected with a turpentine storage tank, and each turpentine storage tank is connected with a turpentine inlet pipe.
Further, a liquid level detector is arranged at the upper end of the inner wall of the inner tank body, and the liquid level detector controls the spiral blanking device.
Further, a liquid discharge groove is arranged at the bottom of the inner tank body, and the bottom of the liquid discharge groove is connected with the lower end of the fat liquid discharge pipe.
Further, filter screens are arranged in the high-level cylinder and the transition cylinder.
Further, a guide plate is arranged at the fat inlet at the upper end inside the clarifying tank, and a guide opening is formed between the lower end of the guide plate and the inner wall of the clarifying tank.
Further, the middle lower parts of the two adjacent clarifying tanks are connected through a grease discharging pipe, and the grease discharging pipe is provided with a switch valve.
The turpentine raw materials enter from a raw material inlet on the mixing box, hot water in the solar water heating device and turpentine in the turpentine storage tank are simultaneously introduced into the mixing box, the temperature of the solar hot water is high, a part of turpentine raw materials can be rapidly dissolved, and the dissolution efficiency is greatly increased. The mixed raw materials are conveyed and discharged through a spiral discharging device, and the conveying process promotes the mixing and dissolution of the raw materials again. And high-temperature rosin enters the inner tank body, after the liquid level reaches a liquid level detector, the liquid level detector feeds information back to the spiral feeder, the spiral feeder stops conveying, and at the moment, the switch valves on the mixed raw material inlet pipe, the steam inlet pipe and the hot water inlet are closed. The high-temperature steam generated in the steam generating device enters the inner tank body from the steam inlet, the rosin is discharged from the steam outlet pipe after being heated, meanwhile, the motor starts to work, the rotating propeller is driven to rotate, hot oil starts to be introduced into the hot oil coil pipe, and the rosin in the inner tank body is circularly heated. The hot water in the solar water heating device is introduced into the steam generating device, so that the energy consumption required by steam generation is reduced. The rosin is quickly heated and dissolved in the inner tank body, and the rotating paddles stir the rosin in the inner tank body, so that the rosin is heated uniformly, the rosin is fully dissolved, and impurities in the rosin fall on the impurity removal grid to be blocked. The power generated by the rotation of the rosin driven by the propeller continuously flushes impurities on the impurity removal grid, and the residual rosin on the impurities is fully dissolved. After the dissolution is finished, the motor stops working, the switch valves on the steam inlet, the hot water inlet, the mixed raw material inlet pipe and the steam outlet pipe are closed, the switch valves on the steam inlet pipe and the fat liquor outlet pipe are opened, the steam inlet pipe is filled with steam, and the fat liquor in the inner tank body is pressed into the fat liquor outlet pipe to be discharged. The liquid draining groove is arranged, so that the fat liquid in the inner tank body can be fully drained. After the grease liquid is discharged, a foreign matter removing valve is opened, impurities on a foreign matter removing grid are removed, the grease liquid is placed into a slag hopper, lifted by a lifting device and falls into an oil volatilization device, turpentine attached to the impurities is volatilized through high-temperature steam heating, and the turpentine flows back into a mixing box for recycling through a turpentine inlet pipe. In the heating dissolving and fat liquid discharging process, if the pressure in the inner tank body reaches a dangerous value, the safety pressure release valve automatically pops open to release pressure. The steam discharged from the steam outlet pipe contains some volatilized turpentine, and the turpentine is cooled by the cooling device and flows into the mixing box for recycling.
The fat liquid extruded by the steam enters the high-level cylinder from the fat liquid discharge pipe, the high-level cylinder can lighten the pressure of the fat liquid extruded from the dissolving tank, and the fat liquid entering at high pressure can be buffered and filtered by the filter screen and then enters the clarifying tank. After entering the clarifier, the guide plate guides the grease to flow downwards along the inner wall of the clarifier from the guide opening, and the excessive impact on the original grease in the clarifier is avoided. When the fat liquid is deposited in the clarifying tank, the switch valve on the fat discharging pipe is closed. Impurities and moisture in the fat liquid are deposited downwards, and the upper layer liquid level is rosin. After the liquid level of the rosin reaches the overflow pipe, the rosin starts to flow into the next clarifying tank, and the rosin is continuously introduced until all the clarifying tanks are fully filled. After clarification, a switch valve on the lipid discharging pipe is opened, lipid liquid above the lipid discharging pipe flows into the next clarification tank, and the lipid liquid in the last clarification tank flows into the transition cylinder after being heated by high-temperature steam, and flows into the preheating pot after being filtered. When all the grease in the clarifying tank flows to a position below the grease discharging pipe, a sedimentation outlet is opened, and impurities deposited at the bottom of the clarifying tank and part of water are discharged. And then closing the precipitation outlet, introducing hot water into the dissolution tank, pressing the hot water into the clarification tank by utilizing high-pressure steam, and completely discharging all the residual lipid liquid in the clarification tank only by reaching the position below the lipid discharging pipe, thereby saving the consumption of the hot water. The discharged fat liquid is heated by high-temperature steam in the tail end clarifying tank, then is introduced into a preheating pot for continuous heating, the temperature of the fat liquid in the preheating pot is quickly raised by heating, the temperature can reach 120-140 ℃, and a large amount of turpentine volatilizes and water evaporates at the moment and is discharged from an outlet at the upper end. Simultaneously, the fat liquid in the preheating pot continuously enters the distillation tower from the lower end, the fat liquid in the distillation tower is heated again and rapidly rises in temperature to 180-200 ℃, and turpentine and water in the fat liquid in the distillation tower are completely discharged from the upper end of the distillation tower after a period of time. Turpentine and water discharged from the upper ends of the preheating pot and the distillation tower are cooled by a spiral heat exchanger, and after being separated by an oil-water separator, the turpentine enters a turpentine storage tank for storage. And (5) introducing the rosin finally prepared by the distillation tower into a rosin storage tank for storage.
The invention has the beneficial effects that:
(1) According to the invention, the solar hot water is mixed with the raw material rosin, so that the temperature of the mixed material is increased, the heating time of subsequent dissolution is reduced, and the dissolution efficiency is improved; the high-temperature steam is prepared by heating solar hot water, so that the energy consumption is saved; the solar hot water is heated by solar energy, so that the environment is protected, the energy consumption is reduced, and the cost is reduced;
(2) According to the invention, the hot oil coil pipe is added outside the inner tank body, so that the dissolution efficiency of rosin is increased, the stability of dissolution temperature is ensured, and the dissolution effect is improved; the hot oil in the hot oil coil is heated by solar hot water, so that the energy consumption is reduced;
(3) When the dissolving process is carried out, the rotating paddles in the inner tank body can improve the heating speed of the rosin, so that the rosin is heated uniformly, and the rosin attached to impurities can be washed, so that the dissolving effect is improved;
(4) According to the invention, a large amount of turpentine attached to impurities can be recovered and reused after the dissolving process is finished, so that the production cost is saved;
(5) When rosin is introduced into the clarifying tank, the rosin is left along the inner wall of the clarifying tank, so that the impact force on the rosin in the clarifying tank is small, the sedimentation effect is good, the efficiency is high, the horizontal arrangement quantity of the clarifying tanks can be reduced according to the situation, and the manufacturing cost of equipment is increased;
(6) After clarification, the water level introduced into the clarifying tank can completely discharge all the residual lipid in the clarifying tank only by reaching the position below the lipid discharging pipe, so that the hot water consumption is saved;
(7) The distillation process of the invention is three-stage heating, namely high-temperature steam heating and heat preservation in the tail end clarifying tank, heating and temperature rising in the preheating pot, and reheating and temperature rising in the distillation tower, thereby improving the distillation efficiency and effect.
Drawings
FIG. 1 is a schematic diagram of a rosin production processing system;
FIG. 2 is a schematic diagram of the results of a dissolution apparatus;
FIG. 3 is an enlarged view at B of FIG. 1;
the device comprises a 1-dissolving device, a 101-outer tank body, a 102-inner tank body, a 103-interlayer, a 104-hot oil coil pipe, a 105-impurity removal grid, a 106-impurity removal valve, a 107-propeller, a 108-motor, a 109-steam inlet, a 110-hot water inlet, a 111-mixed raw material inlet pipe, a 112-steam outlet pipe, a 113-steam inlet pipe, a 114-fat liquor discharge pipe, a 115-mixing tank, a 116-screw feeder, a 117-raw material inlet, a 118-solar hot water pipe, a 119-turpentine inlet pipe, a 120-return pipe, a 121-cooling device, a 122-liquid discharge tank, a 123-liquid level detector, a 2-solar hot water device, a 3-steam generating device, a 4-hot oil device, a 5-slag hopper, a 6-lifting device, a 7-oil volatilization device, an 8-high-position cylinder, a 9-clarifying tank, a 901-fat inlet, a 902-deflector, a 10-position 11-fat discharge pipe, a 12-sedimentation outlet, a 13-transition cylinder, a 14-preheating pot, a 15-distillation tower, a 16-oil-storage tank, a 17-heat exchanger, a 17-spiral heat exchanger, a 18-turpentine separator and a 19-oil-storage tank.
Detailed Description
As shown in fig. 1, a rosin production and processing system comprises a dissolving device 1, a solar water heating device 2, a steam generating device 3, a hot oil device 4, a slag hopper 5, a lifting device 6, an oil volatilizing device 7, a high-level cylinder 8, a clarifying tank 9, an overflow pipe 10, a precipitation outlet 12, a transition cylinder 13, a preheating pot 14, a distillation tower 15, a rosin storage tank 16, a spiral heat exchanger 17, an oil-water separator 18 and a turpentine storage tank 19;
as shown in fig. 2, the dissolving device 1 comprises an outer tank 101, an inner tank 102, an interlayer 103, a hot oil coil 104, a impurity removing grid 105, an impurity removing valve 106, a rotating propeller 107, a motor 108, a steam inlet 109, a hot water inlet 110, a mixed raw material inlet pipe 111, a steam outlet pipe 112, a steam inlet pipe 113, a fat liquor discharge pipe 114, a mixing box 115 and a cooling device 121, wherein the inner tank 102 is arranged in the outer tank 101, the interlayer 103 is formed between the outer tank 101 and the inner tank 102, the hot oil coil 104 is arranged in the interlayer 103, the impurity removing grid 105 is arranged in the inner tank 102, the rotating propeller 107 is arranged below the impurity removing grid 105, the rotating propeller 107 is connected with the motor 108, the motor 108 is arranged below the outer tank 101, the upper end of the outer tank 101 is provided with a safety valve 123, the lower end of the inner tank 102 is provided with the steam inlet 109, the upper end of the inner tank 102 is provided with the hot water inlet 110, the mixed raw material inlet pipe 111, the steam outlet pipe 112, the steam inlet 113, the steam inlet pipe 113, the steam outlet pipe 114, the steam inlet pipe 114 and the steam outlet pipe 114 are arranged at the lower end of the inner tank 102, the upper end of the steam inlet pipe 114 is extended to the upper end of the steam inlet pipe 114, the upper end of the steam inlet pipe 114 is arranged above the steam inlet pipe 114, the steam inlet pipe 114 is extended to the lower end of the steam inlet pipe 114, the steam inlet pipe 114 is arranged above the steam inlet pipe 114, and the upper end of the mixed raw material inlet pipe 114 is arranged at the lower end of the steam inlet pipe 114, and the steam inlet pipe is arranged at the lower end of the steam, and is connected;
the hot water inlet 110 is connected with the solar water heating device 2;
the steam inlet 109 and the steam inlet pipe 113 are connected with the steam generating device 3, and the steam generating device 3 is connected with the solar water heating device 2;
the two ends of the hot oil coil 104 are connected with a hot oil device 4, an annular coil is arranged around the hot oil device 4, and the two ends of the annular coil are connected with a solar water heating device 2;
the upper end of the mixed raw material inlet pipe 111 is provided with a mixing box 115, a spiral feeder 116 is arranged in the mixing box 115, a raw material inlet 117, a solar hot water pipe 118, a turpentine inlet pipe 119 and a return pipe 120 are arranged above the mixing box 115, and the solar hot water pipe 118 is connected with the solar water heating device 2;
a cooling device 121 is arranged on the steam outlet pipe 112, and the cooling device 121 is connected with a return pipe 120;
the impurity removal valve 106 is externally provided with a slag hopper 5, the slag hopper 5 is connected to the lifting device 6, an oil volatilization device 7 is arranged below the lifting device 6, and the upper end of the oil volatilization device 7 is connected with a turpentine inlet pipe 119 through a pipeline;
the upper end of the fat liquor discharge pipe 114 is connected with the high-level cylinder 8, the lower end of the high-level cylinder 8 is connected with the clarifying tanks 9 through pipelines, a plurality of clarifying tanks 9 are horizontally arranged side by side, the upper ends of two adjacent clarifying tanks 9 are connected through overflow pipes 10, a sedimentation outlet 12 is arranged at the lower end of each clarifying tank 9, a snake-shaped coil is arranged in each tail clarifying tank 9, two ends of each snake-shaped coil are connected with the steam generating device 3, the tail-end clarifying tank 9 is connected with the transition cylinder 13, the lower end of the transition cylinder 13 is connected with the preheating pot 14 through a pipeline, the lower end of the preheating pot 14 is connected with the distillation tower 15 through a pipeline, the lower end of the distillation tower 15 is connected with the rosin storage tank 16 through a pipeline, the preheating pot 14 and the upper end of the distillation tower 15 are connected with the spiral heat exchanger 17 through pipelines, the spiral heat exchanger 17 is connected with the oil-water separator 18, the oil-water separator 18 is connected with the turpentine storage tank 19, and the turpentine storage tank 19 is connected with the turpentine inlet pipe 119.
The upper end of the inner wall of the inner tank 102 is provided with a liquid level detector 123, and the liquid level detector 123 controls the screw feeder 116.
The bottom of the inner tank 102 is provided with a drain tank 122, and the bottom of the drain tank 122 is connected with the lower end of the fat liquor discharge pipe 114.
Filter screens are arranged in the high-level cylinder 8 and the transition cylinder 13.
As shown in fig. 3, a baffle 902 is disposed at a fat inlet 901 at the upper end of the interior of the clarifier 9, and a flow guide port is formed between the lower end of the baffle 902 and the inner wall of the clarifier 9.
The middle lower parts of the two adjacent clarifying tanks 9 are connected through a grease discharging pipe 11, and the grease discharging pipe 11 is provided with a switch valve.
Claims (6)
1. The rosin production and processing system is characterized by comprising a dissolving device (1), a solar water heating device (2), a steam generating device (3), a hot oil device (4), a slag hopper (5), a lifting device (6), an oil volatilization device (7), a high-level cylinder (8), a clarifying tank (9), an overflow pipe (10), a sedimentation outlet (12), a transition cylinder (13), a preheating pot (14), a distillation tower (15), a rosin storage tank (16), a spiral heat exchanger (17), an oil-water separator (18) and a turpentine storage tank (19);
dissolving device (1) including outer jar body (101), interior jar body (102), intermediate layer (103), hot oil coil pipe (104), edulcoration grid (105), edulcoration valve (106), screw (107), motor (108), steam inlet (109), hot water inlet (110), mixed raw materials advances pipe (111), steam exit tube (112), steam advances pipe (113), fat liquid discharge pipe (114), mixing box (115) and cooling device (121), be provided with interior jar body (102) in outer jar body (101), form intermediate layer (103) between outer jar body (101) and the interior jar body (102), be provided with hot oil coil pipe (104) in intermediate layer (103), be provided with edulcoration grid (105) in interior jar body (102), be provided with edulcoration valve (106) on the lateral wall of interior jar body (102) of edulcoration grid (105) top, be provided with screw (107) below edulcoration grid (105), screw (107) are being connected motor (108), and motor (108) set up in outer jar body (101) below, outer jar body (101) upper end is provided with hot water inlet (102), and inner tank (102) are provided with the pressure release end (102) The mixed raw material inlet pipe (111), the steam outlet pipe (112), the steam inlet pipe (113) and the fat liquor outlet pipe (114), wherein the steam inlet (19), the hot water inlet (110), the mixed raw material inlet pipe (111), the steam outlet pipe (112), the steam inlet pipe (113) and the fat liquor outlet pipe (114) are respectively provided with a switch valve, and the lower end of the fat liquor outlet pipe (114) extends to the bottom of the inner tank body (102);
the hot water inlet (110) is connected with a solar water heating device (2);
the steam inlet (109) and the steam inlet pipe (113) are connected with a steam generating device (3), and the steam generating device (3) is connected with a solar water heating device (2);
the two ends of the hot oil coil pipe (104) are connected with a hot oil device (4), an annular coil pipe is arranged around the hot oil device (4), and the two ends of the annular coil pipe are connected with a solar water heating device (2);
the device is characterized in that a mixing box (115) is arranged at the upper end of the mixed raw material inlet pipe (111), a spiral blanking device (116) is arranged in the mixing box (115), a raw material inlet (117), a solar hot water pipe (118), a turpentine inlet pipe (119) and a return pipe (120) are arranged above the mixing box (115), and the solar hot water pipe (118) is connected with a solar hot water device (2);
a cooling device (121) is arranged on the steam outlet pipe (112), and the cooling device (121) is connected with a return pipe (120);
the impurity removing valve (106) is externally provided with a slag hopper (5), the slag hopper (5) is connected to the lifting device (6), an oil volatilization device (7) is arranged below the lifting device (6), and the upper end of the oil volatilization device (7) is connected with a turpentine inlet pipe (119) through a pipeline;
the utility model discloses a turpentine storage tank, including fat liquor discharge pipe (114), high-order section of thick bamboo (8) is being connected to fat liquor discharge pipe (114) upper end, high-order section of thick bamboo (8) lower extreme is being connected through pipe connection clarifier (9), clarifier (9) level is being provided with a plurality of side by side, two adjacent clarifier (9) upper ends are being connected through overflow pipe (10), every clarifier (9) lower extreme is provided with sedimentation outlet (12), be provided with serpentine coil in terminal clarifier (9), steam generator (3) are being connected at serpentine coil both ends, transition section of thick bamboo (13) are being connected to terminal clarifier (9), transition section of thick bamboo (13) lower extreme is being connected through pipe connection preheating pot (14), preheating pot (14) lower extreme is being connected through pipe connection distillation column (15), distillation column (15) lower extreme is being connected through pipe connection rosin holding vessel (16), preheating pot (14) and distillation column (15) upper end are being connected through pipe connection spiral heat exchanger (17), spiral heat exchanger (17) are being connected oil water separator (18), turpentine holding vessel (19) are being connected in oil water separator (18), turpentine holding vessel (19) are being connected turpentine oil in (119).
2. The rosin production processing system of claim 1, wherein a liquid level detector (123) is provided at the upper end of the inner wall of the inner tank (102), and the liquid level detector (123) controls the screw feeder (116).
3. The rosin production processing system of claim 1, wherein a drain tank (122) is provided at the bottom of the inner tank (102), and the bottom of the drain tank (122) is connected to the lower end of the fat liquor drain pipe (114).
4. Rosin production processing system according to claim 1, characterized in that screens are provided in the high-level cylinder (8) and the transition cylinder (13).
5. The rosin production processing system according to claim 1, wherein a deflector (902) is arranged at a fat inlet (901) at the upper end of the interior of the clarifying tank (9), and a deflector opening is formed between the lower end of the deflector (902) and the inner wall of the clarifying tank (9).
6. Rosin production processing system according to claim 1, characterized in that the middle lower parts of the two adjacent clarifying tanks (9) are connected through a grease discharging pipe (11), and the grease discharging pipe (11) is provided with a switch valve.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611200232.7A CN106675415B (en) | 2016-12-22 | 2016-12-22 | Rosin production system of processing |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201611200232.7A CN106675415B (en) | 2016-12-22 | 2016-12-22 | Rosin production system of processing |
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| CN106675415A CN106675415A (en) | 2017-05-17 |
| CN106675415B true CN106675415B (en) | 2023-06-23 |
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| CN113559538B (en) * | 2021-09-01 | 2023-04-25 | 广西上林县林发松香有限公司 | Rosin processing equipment and processing method thereof |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104194636A (en) * | 2014-09-03 | 2014-12-10 | 松阳县永新机械制造有限公司 | Colophony production equipment |
| CN105617944A (en) * | 2016-03-21 | 2016-06-01 | 南京林业大学 | Vertical continuous pine resin dry-process melting device |
| CN205462140U (en) * | 2016-02-24 | 2016-08-17 | 安远县松远林业化工有限公司 | Multi -functional rosin production liquates cauldron |
-
2016
- 2016-12-22 CN CN201611200232.7A patent/CN106675415B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104194636A (en) * | 2014-09-03 | 2014-12-10 | 松阳县永新机械制造有限公司 | Colophony production equipment |
| CN205462140U (en) * | 2016-02-24 | 2016-08-17 | 安远县松远林业化工有限公司 | Multi -functional rosin production liquates cauldron |
| CN105617944A (en) * | 2016-03-21 | 2016-06-01 | 南京林业大学 | Vertical continuous pine resin dry-process melting device |
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