CN216604081U - Brominated butyl rubber's solvent recovery system - Google Patents
Brominated butyl rubber's solvent recovery system Download PDFInfo
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- CN216604081U CN216604081U CN202121540970.2U CN202121540970U CN216604081U CN 216604081 U CN216604081 U CN 216604081U CN 202121540970 U CN202121540970 U CN 202121540970U CN 216604081 U CN216604081 U CN 216604081U
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Abstract
The utility model provides a solvent recovery system for brominated butyl rubber, which comprises: a flash tank; the gas inlet of the first condenser is communicated with a gas outlet at the top of the flash tank; the liquid inlet of the solvent recovery tank is communicated with the liquid outlet of the first condenser; the feed inlet of the first-stage vacuum stripping tower is communicated with the discharge outlet of the flash tank; the feeding hole of the second-stage vacuum stripping tower is communicated with the discharging hole of the first-stage vacuum stripping tower; a first liquid ring vacuum pump system in communication between the primary vacuum stripper and the solvent recovery tank; a second liquid ring vacuum pump system in communication between the secondary vacuum stripper and the solvent recovery tank. The solvent recovery system adopts electricity as a power source, so that the energy consumption is greatly saved, the solvent stripping effect is better, the solvent recovery rate is improved, the hexane content in the subsequent glue and water is reduced, the harm brought to the subsequent way is reduced, the load of tail gas treatment is reduced, and the environmental protection pressure is reduced.
Description
Technical Field
The utility model relates to the field of brominated butyl rubber, in particular to a solvent recovery system of brominated butyl rubber.
Background
Brominated butyl rubber (BIIR for short) is an important modified product of common butyl rubber (IIR for short), which not only retains double bonds in the molecular structure of common IIR and keeps the original characteristics of IIR, but also improves the reactivity of the IRR and improves the self-adhesiveness, mutual adhesiveness, and the compatibility and co-vulcanization of IIR and unsaturated rubber by connecting bromine atoms in the molecular structure of the IRR. After IIR bromination, crosslinking active points are increased, and the reactivity of double bonds is enhanced. BIIR still has the advantages of high barrier property, high aging resistance, high heat resistance, high damping property, good sound absorption property and the like of the RI. Meanwhile, the method has the characteristics which are not possessed by the multi-aspect RI R, is widely applied to various fields, and is being paid attention to in various aspects in processing and application. BIIR is one of the representatives of high-performance and high-value-added synthetic rubbers, is a new strategic material, and is widely used in tubeless tires of automobiles, medical products and rubber industrial products.
With the continuous expansion of BIIR production scale, the product quality is improved, the yield is improved, and meanwhile, the problems of energy conservation, consumption reduction and environmental protection cannot be ignored. The main production process flow of BIIR is (see figure 1): a glue solution tank working section, a dehydration working section, a halogenation feeding preparation working section, a halogenation reaction and neutralization working section, a solvent recovery working section, a water recovery and circulation working section, an additive preparation working section and a discharged gas washing tower working section. Wherein, the solvent recovery section mainly comprises a hexane removal process, hexane is evaporated and removed for recovery, the glue solution becomes colloidal particle water again and is conveyed to a post-treatment drying section for drying and the like. In the working section, the removal degree of hexane in the glue solution determines the length of the production operation period, the unit consumption of hexane, whether the tail gas reaches the standard or not, and the like. Actual engineering experience shows that when the hexane removal effect is poor in the process, the content of residual hexane in the glue solution is high, the glue is sticky, easy to hang on the wall and easy to block a pump, the reduction or forced shutdown is caused, and the overall production efficiency is seriously influenced; the hexane content in the glue neutralization water is high, and the glue neutralization water enters an aftertreatment workshop along with the process flow, so that great harm is brought to the health of people; poor solvent recovery effects can directly affect energy consumption cost, and the profit of the final product is obviously reduced.
Disclosure of Invention
In view of the above, the present invention is directed to a solvent recovery system for brominated butyl rubber. The solvent recovery system provided by the utility model can effectively reduce the hexane content in glue and water, so that the solvent recovery rate is maximized, and finally the tail gas reaches the standard and is discharged.
The utility model provides a solvent recovery system for brominated butyl rubber, which comprises:
a flash tank;
the gas inlet of the first condenser is communicated with a gas outlet at the top of the flash tank;
the liquid inlet of the solvent recovery tank is communicated with the liquid outlet of the first condenser;
the feed inlet of the first-stage vacuum stripping tower is communicated with the discharge outlet of the flash tank;
the feed inlet of the second-stage vacuum stripping tower is communicated with the discharge outlet of the first-stage vacuum stripping tower;
a first liquid ring vacuum pump system in communication between the primary vacuum stripper and the solvent recovery tank;
a second liquid ring vacuum pump system in communication between the secondary vacuum stripper and the solvent recovery tank.
In one embodiment of the present invention, further comprising: a flash drum pump in communication between the flash drum and the primary vacuum stripper.
In one embodiment of the present invention, further comprising: and the primary stripping pump is communicated between the primary vacuum stripping tower and the secondary vacuum stripping tower.
In one embodiment of the present invention, further comprising: a secondary stripping pump in communication between the secondary vacuum stripper and a downstream post-treatment section of the solvent recovery system.
In one embodiment of the utility model, the bottom of the flash tank is provided with an agitator.
In one embodiment of the utility model, the bottom of the primary vacuum stripping tower is provided with a stirrer.
In one embodiment of the utility model, the bottom of the secondary vacuum stripper is provided with a stirrer.
The utility model provides a solvent recovery system of brominated butyl rubber, which comprises: a flash tank; the gas inlet of the first condenser is communicated with a gas outlet at the top of the flash tank; the liquid inlet of the solvent recovery tank is communicated with the liquid outlet of the first condenser; the feed inlet of the first-stage vacuum stripping tower is communicated with the discharge outlet of the flash tank; the feeding hole of the second-stage vacuum stripping tower is communicated with the discharging hole of the first-stage vacuum stripping tower; a first liquid ring vacuum pump system in communication between the primary vacuum stripper and the solvent recovery tank; a second liquid ring vacuum pump system in communication between the secondary vacuum stripper and the solvent recovery tank. The solvent recovery system adopts electricity as a power source, so that the energy consumption is greatly saved; moreover, the solvent stripping effect of the solvent recovery system is better, the solvent recovery rate is improved, the content of hexane in subsequent rubber products and water is reduced, the harm brought to a subsequent path is reduced, the load of tail gas treatment is reduced, and the environmental protection pressure is reduced; and the hexane solvent with more recovery amount can be put into the upstream working section again for use, so that the unit consumption of hexane is reduced.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the provided drawings without creative efforts.
FIG. 1 is a flow diagram of a process for producing brominated butyl rubber;
FIG. 2 is a schematic diagram of a solvent recovery system for brominated butyl rubber provided in accordance with an embodiment of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be obtained by a person skilled in the art without making any creative effort based on the embodiments in the present invention, belong to the protection scope of the present invention.
The utility model provides a solvent recovery system for brominated butyl rubber, which comprises:
a flash tank;
the gas inlet of the first condenser is communicated with a gas outlet at the top of the flash tank;
the liquid inlet of the solvent recovery tank is communicated with the liquid outlet of the first condenser;
the feed inlet of the first-stage vacuum stripping tower is communicated with the discharge outlet of the flash tank;
the feeding hole of the second-stage vacuum stripping tower is communicated with the discharging hole of the first-stage vacuum stripping tower;
a first liquid ring vacuum pump system in communication between the primary vacuum stripper and the solvent recovery tank;
a second liquid ring vacuum pump system in communication between the secondary vacuum stripper and the solvent recovery tank.
Referring to fig. 1, fig. 1 is a flow chart of a production process of brominated butyl rubber, and the present invention provides a solvent recovery system (i.e., a solvent stripping system) of brominated butyl rubber for a solvent recovery section thereof. Referring to fig. 2, fig. 2 is a schematic diagram of a solvent recovery system for brominated butyl rubber according to one embodiment of the present invention. Wherein, 1 is the flash tank, 1a is the agitator, 2 is first condenser, 3 is the solvent recovery jar, 4 is first order vacuum stripping tower, 4a is the agitator, 4b is first liquid ring vacuum pump system, 5 is second grade vacuum stripping tower, 5b is second liquid ring vacuum pump system, 1-L-4 is the flash tank pump, 4-L-5 is the first order stripping pump, 5d is the second grade stripping pump.
According to the utility model, the flash tank 1 is in communication with an upstream neutralization section of a BIIR production process, receives BIIR glue solution from the upstream section, and performs solvent flash on the BIIR glue solution. In some embodiments of the utility model, the feed inlet to the flash tank 1 is at the upper or top of the flash tank 1. After the BIIR glue solution in the upstream section enters the flash tank 1 from the upper part or the top of the flash tank 1, the solvent in the BIIR glue solution is converted into gas to ascend along the flash tank 1 through flash evaporation, and the BIIR glue solution without the solvent descends along the flash tank 1 and is enriched at the bottom of the flash tank 1, so that the separation of the solvent and the BIIR glue solution is realized. In actual operation, the operating temperature of the flash tank 1 is 80-120 ℃.
In some embodiments of the utility model, the bottom of the flash tank 1 is provided with an agitator 1 a. The stirrer 1a comprises a stirring shaft, a motor connected to one end of the stirring shaft and a stirring paddle connected to the other end of the stirring shaft; wherein, the (mixing) shaft is vertical to stretch into in the flash tank from the bottom of flash tank 1, and the one end of connecting the stirring leaf is in flash tank 1. Above-mentioned agitator 1a continuously stirs at flash tank 1 operation in-process, makes the material homodisperse in the flash tank 1, makes the abundant flash distillation of solvent, is favorable to promoting the solvent rate of recovery. In some embodiments of the utility model, the bottom of the flash tank 1 is provided with a discharge port for discharging the BIIR glue solution enriched at the bottom.
According to the utility model, the gas inlet of the first condenser 2 is communicated with the gas outlet at the top of the flash tank 1 and is used for receiving the solvent gas discharged from the top of the flash tank 1 and condensing the solvent gas into liquid.
According to the utility model, a liquid inlet of the solvent recovery tank 3 is communicated with a liquid outlet of the first condenser 2, and the first condenser 2 condenses the solvent gas discharged from the top of the flash tank 1 into liquid and then sends the liquid to the solvent recovery tank 3 to recover the solvent.
According to the utility model, the feed inlet of the primary vacuum stripping tower 4 is communicated with the discharge outlet of the flash tank 1 and is used for receiving BIIR glue solution which is flashed from the flash tank 1 and stripping the BIIR glue solution. In some embodiments of the utility model, the feed inlet of the primary vacuum stripper 4 is in the upper or middle part of the primary vacuum stripper 4. After the glue solution in the flash tank 1 enters the first-stage vacuum stripping tower 4, the solvent in the BIIR glue solution is further converted into gas through steam stripping, the gas goes upwards along the first-stage vacuum stripping tower 4, the BIIR glue solution without the solvent goes downwards along the first-stage vacuum stripping tower 4 and is enriched at the bottom of the tower, and the separation of the solvent and the BIIR glue solution is further realized. In actual operation, the operation temperature of the primary vacuum stripping tower 4 is 75-100 ℃.
In some embodiments of the present invention, a flash tank pump 1-L-4 is further communicated between the flash tank 1 and the primary vacuum stripping tower 4, a feed port of the flash tank pump 1-L-4 is communicated with a discharge port of the flash tank 1, and a discharge port of the flash tank pump 1-L-4 is communicated with a feed port of the primary vacuum stripping tower 4, so as to pump a feed liquid at the bottom of the flash tank 1 into the primary vacuum stripping tower 4.
In some embodiments of the utility model, the bottom of the primary vacuum stripper 4 is provided with a stirrer 4 a. The stirrer 4a comprises a stirring shaft, a motor connected to one end of the stirring shaft and a stirring paddle connected to the other end of the stirring shaft; wherein, the stirring shaft vertically extends into the first-stage vacuum stripping tower 4 from the bottom of the first-stage vacuum stripping tower 4, and one end connected with the stirring blade is positioned in the first-stage vacuum stripping tower 4. Above-mentioned agitator 4a continuously stirs at 4 operation in-process in the one-level vacuum stripping tower, makes material homodisperse in the one-level vacuum stripping tower 4, makes the abundant flash distillation of solvent, is favorable to promoting the solvent rate of recovery. In some embodiments of the present invention, the bottom of the primary vacuum stripping tower 4 is provided with a discharge port for discharging the BIIR glue solution enriched at the bottom.
According to the utility model, a first liquid ring vacuum pump system 4b is communicated between the primary vacuum stripping tower 4 and the solvent recovery tank 3, specifically, a gas inlet of the first liquid ring vacuum pump system 4b is communicated with a gas outlet at the top of the primary vacuum stripping tower 4, and a gas outlet of the first liquid ring vacuum pump system 4b is communicated with an inlet of the solvent recovery tank 3. Provide power through first liquid ring vacuum pump system and improve the vacuum property of one-level vacuum stripping tower 4, the frequency conversion of specific accessible regulating pump improves vacuum property in the tower, make 4 interior solvent gases of one-level vacuum stripping tower fully discharge and collect, be favorable to promoting the solvent recovery effect, reduce the hexane solvent content in follow-up rubber product and the separation aquatic, reduce the aftertreatment degree of difficulty and tail gas treatment load, alleviate the environmental protection pressure, and, liquid ring vacuum pump system adopts the electricity as the power supply, has saved the energy consumption.
The first liquid ring vacuum pump system 4b is a complete set of system, and comprises a liquid ring vacuum pump, a gas-liquid separator, a working liquid cooler (for condensation), an internal piping, an instrument, a valve and the like. The solvent gas discharged from the top of the first-stage vacuum stripping tower 4 is condensed into liquid and discharged.
According to the utility model, the feed inlet of the secondary vacuum stripping tower 5 is communicated with the discharge outlet of the primary vacuum stripping tower 4 and is used for receiving BIIR glue solution from the primary vacuum stripping tower 4 after stripping and carrying out secondary stripping on the BIIR glue solution. In some embodiments of the present invention, the feed inlet of the secondary vacuum stripper 5 is in the upper or middle part of the secondary vacuum stripper 5. After the glue solution in the first-stage vacuum stripping tower 4 enters the second-stage vacuum stripping tower 5, the solvent in the BIIR glue solution is further converted into gas and ascends along the second-stage vacuum stripping tower 5 through stripping, the BIIR glue solution from which the solvent is removed descends along the second-stage vacuum stripping tower 5 and is enriched at the bottom of the tower, and the separation of the solvent and the BIIR glue solution is further realized. In actual operation, the operation temperature of the secondary vacuum stripping tower 5 is 68-80 ℃.
In some embodiments of the present invention, a primary stripping pump 4-L-5 is further communicated between the secondary vacuum stripping tower 5 and the primary vacuum stripping tower 4, a feed port of the primary stripping pump 4-L-5 is communicated with a discharge port of the primary vacuum stripping tower 4, and a discharge port of the primary stripping pump 4-L-5 is communicated with a feed port of the secondary vacuum stripping tower 5, and is configured to pump a feed liquid at the bottom of the primary vacuum stripping tower 4 into the secondary vacuum stripping tower 5.
In some embodiments of the utility model, the bottom of the secondary vacuum stripper 5 is provided with a stirrer 5 a. The stirrer 5a comprises a stirring shaft, a motor connected to one end of the stirring shaft and a stirring paddle connected to the other end of the stirring shaft; wherein, the stirring shaft vertically extends into the second-stage vacuum stripping tower 5 from the bottom of the second-stage vacuum stripping tower 5, and one end connected with the stirring blade is positioned in the second-stage vacuum stripping tower 5. Above-mentioned agitator 5a continuously stirs at 5 operation in-process in the second grade vacuum stripping tower, makes the material homodisperse in the second grade vacuum stripping tower 5, makes the abundant flash distillation of solvent, is favorable to promoting the solvent rate of recovery. In some embodiments of the present invention, the bottom of the secondary vacuum stripping tower 5 is provided with a discharge port for discharging the BIIR glue solution enriched at the bottom.
According to the utility model, a second liquid ring vacuum pump system 5b is communicated between the secondary vacuum stripping tower 5 and the solvent recovery tank 3, specifically, a gas inlet of the second liquid ring vacuum pump system 5b is communicated with a gas outlet at the top of the secondary vacuum stripping tower 5, and a gas outlet of the second liquid ring vacuum pump system 5b is communicated with an inlet of the solvent recovery tank 3. With first liquid ring vacuum pump system 4b with the same reason, provide power through second liquid ring vacuum pump system 5b and improve the vacuum of second grade vacuum stripping tower 5, make the gaseous abundant discharge of second grade vacuum stripping tower 5 interior solvent and collect, be favorable to promoting the solvent recovery effect, reduce the hexane solvent content in follow-up rubber product and the separation aquatic, reduce the aftertreatment degree of difficulty and tail gas treatment load, alleviate the environmental protection pressure, and, liquid ring vacuum pump system adopts the electricity as the power supply, has saved the energy consumption.
Like the first liquid ring vacuum pump system 4b, the second liquid ring vacuum pump system 5b is a complete system including a liquid ring vacuum pump, a gas-liquid separator, a working fluid cooler (for condensation), an internal piping, a meter, a valve, and the like. The solvent gas discharged from the top of the secondary vacuum stripping tower 5 is condensed into liquid to be discharged after being collected.
In some embodiments of the utility model, further comprising: and the secondary stripping pump 5d is communicated between the secondary vacuum stripping tower 5 and the downstream post-treatment section of the solvent recovery system, a feed inlet of the secondary stripping pump 5d is communicated with a discharge outlet of the secondary vacuum stripping tower 5, and a discharge outlet of the secondary stripping pump 5d is communicated with the downstream post-treatment section and is used for pumping the material liquid at the bottom of the secondary vacuum stripping tower 5 to the downstream post-treatment section for post-treatment.
The existing solvent recovery system has the following problems: the system has insufficient stripping capacity, poor solvent recovery effect and high unit consumption of hexane; in addition, the hexane is brought to a back path, so that the health of operators in a post-treatment workshop is damaged, and the load of tail gas treatment is increased; the content of hexane in the colloidal particles and water in the secondary stripping tower is higher; the content of non-methane total hydrocarbons in tail gas components is high, so that the tail gas absorption effect is influenced; fourthly, the medium pressure steam consumption of the power source is high, and the energy consumption is high. The solvent recovery system for brominated butyl rubber provided by the utility model adopts electricity as a power source, so that the energy consumption is greatly saved; moreover, the solvent stripping effect of the solvent recovery system is better, the solvent recovery rate is improved, the content of hexane in subsequent rubber products and water is reduced, the harm brought to a subsequent path is reduced, the load of tail gas treatment is reduced, and the environmental protection pressure is reduced; and the hexane solvent with more recovery amount can be put into the upstream working section again for use, so that the unit consumption of hexane is reduced. Specifically, the method comprises the following steps: the vacuum degree of the first-stage stripping tower and the second-stage stripping tower is obviously improved, and a better vacuum effect is achieved; the residual quantity of hexane in the glue neutralization water is obviously reduced; the stripping recovery effect of hexane is improved, and the unit consumption of the hexane is reduced by 5-11 kg/t of glue; fourthly, the content of non-methane total hydrocarbon in the post-treatment tail gas is reduced, which is more beneficial to the operation of a tail gas treatment device; fifth, medium-pressure steam consumption is saved, circulating water consumption is reduced, and cooling load is reduced; sixthly, the operation is more convenient.
Example 1
Carrying out cationic polymerization on isobutene and isoprene to obtain IIR basic colloidal particle water, conveying the IIR basic colloidal particle water to a halogenated feeding storage tank through a colloidal particle water pump, carrying out extrusion dehydration through a vibrating screen and a screw machine, carrying out colloidal concentration preparation through cold and hot hexane, carrying out bromination reaction according to the set colloidal concentration, and carrying out neutralization on residual bromine and hydrogen bromide by using a neutralization solution to obtain BIIR colloidal solution. And (3) passing the BIIR glue solution through a coagulation system, then entering a solvent recovery system (as shown in figure 2) of the utility model, carrying out solvent stripping recovery, and sending the obtained colloidal particle water to a post-treatment drying unit for dehydration, drying and packaging.
Comparative example 1
The solvent recovery system of example 1 was replaced with a vacuum ejector system using medium-pressure steam as a power source, and the procedure of example 1 was followed in the same manner as in example 1. The results show that the vacuum injection system adopting medium-pressure steam as a power source has poor hexane stripping effect, and the hexane content in the glue and the water is high; the medium-pressure steam consumption is large, and the circulating water consumption is large; the colloidal particle water is sent to a post-treatment drying unit for dehydration, drying and packaging, and the tail gas treatment device has high NMHC content.
See table 1 for a comparison of the effects of example 1 and comparative example 1.
Table 1 effects of example 1 and comparative example 1
The operation parameters of the stripping tower, the hexane consumption, the hexane content in glue and water and the NMHC content data result of tail gas show that the solvent stripping recovery system provided by the utility model can effectively reduce the energy consumption, greatly improve the hexane recovery effect, reduce the hexane consumption of BIIR products, reduce the total product cost, discharge the tail gas up to the standard and meet the environmental protection requirement.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (7)
1. A solvent recovery system for brominated butyl rubber, comprising:
a flash tank;
the gas inlet of the first condenser is communicated with a gas outlet at the top of the flash tank;
the liquid inlet of the solvent recovery tank is communicated with the liquid outlet of the first condenser;
the feed inlet of the first-stage vacuum stripping tower is communicated with the discharge outlet of the flash tank;
the feeding hole of the second-stage vacuum stripping tower is communicated with the discharging hole of the first-stage vacuum stripping tower;
a first liquid ring vacuum pump system in communication between the primary vacuum stripper and the solvent recovery tank;
a second liquid ring vacuum pump system in communication between the secondary vacuum stripper and the solvent recovery tank.
2. The solvent recovery system of claim 1, further comprising: a flash drum pump in communication between the flash drum and the primary vacuum stripping column.
3. The solvent recovery system of claim 1, further comprising: and the primary stripping pump is communicated between the primary vacuum stripping tower and the secondary vacuum stripping tower.
4. The solvent recovery system of claim 1, further comprising: a secondary stripping pump in communication between the secondary vacuum stripper and a downstream post-treatment section of the solvent recovery system.
5. The solvent recovery system of claim 1, wherein a bottom of the flash tank is provided with an agitator.
6. The solvent recovery system of claim 1, wherein the primary vacuum stripper is provided with a stirrer at the bottom.
7. The solvent recovery system of claim 1, wherein the bottom of the secondary vacuum stripper is provided with an agitator.
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| CN115068966A (en) * | 2022-08-22 | 2022-09-20 | 淄博鲁华泓锦新材料集团股份有限公司 | Continuous desolventizing and refining method for hydrogenated petroleum resin |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115068966A (en) * | 2022-08-22 | 2022-09-20 | 淄博鲁华泓锦新材料集团股份有限公司 | Continuous desolventizing and refining method for hydrogenated petroleum resin |
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