CN203741272U - Production system of modified pitch - Google Patents
Production system of modified pitch Download PDFInfo
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- CN203741272U CN203741272U CN201420039252.0U CN201420039252U CN203741272U CN 203741272 U CN203741272 U CN 203741272U CN 201420039252 U CN201420039252 U CN 201420039252U CN 203741272 U CN203741272 U CN 203741272U
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Abstract
The utility model relates to a production system of modified pitch. The production system comprises a modified intermediate pitch processing device and a moderate-temperature pitch modification reaction device connected with the modified intermediate pitch processing device, wherein the modified intermediate pitch processing device comprises a vacuum flasher, a heavy oil cooler, a heavy oil separator, a heavy oil sealing tank, a heavy oil storage tank, a vacuum condenser and a vacuum tank; the moderate-temperature pitch modification reaction device comprises a pitch heat exchanger, a pitch sealing tank connected with the heat exchanger, a pitch pump connected with the pitch sealing tank, a modification reactor connected to the pitch pump, a pitch heat exchanger connected to the modification reactor and a hot-molten salt heat supply system connected to the modification reactor and the pitch heat exchanger. The production system of modified pitch disclosed by the utility model has the advantages that the structure is reasonable, energy conservation and high efficiency are achieved, various indexes of pitch are significantly improved, the energy and power consumption are greatly reduced and no pollutant leakage in the entire reaction process is ensured.
Description
Technical field
The utility model relates to modified pitch production technical field, particularly a kind of co-generation system of modified pitch.
Background technology
Hard pitch and modified pitch are taking mid-temperature pitch as raw material, make through respective handling.Mainly contain oxidation thermal polymerization method, normal pressure thermal polymerization method, pressurization thermal polymerization method, vacuum flashing method etc. taking pitch as the production method of raw material production modified pitch.
Oxidation thermal polymerization method is that pitch is packed in the reactor with heating unit, react to passing into pressurized air in reactor, the subject matter of the method is the relation that is difficult to height with the quinoline insolubles content of balance modified pitch softening temperature, is difficult to produce qualified product.
Normal pressure thermal polymerization method is the at present domestic a kind of method generally adopting, although this method can obtain satisfied product, but owing to using fuel combustion flue gas heating polymeric kettle, the flow velocity of its flue gas is very fast, enthalpy is lower, the thermo-efficiency of heat-processed is low, energy expenditure is large, and easily causes the material in reactor inequality of being heated, local superheating and coking.
Pressurization thermal polymerization method, except having the shortcoming of normal pressure thermal polymerization method, adopts high-tension apparatus to cause the shortcoming of equipment investment increase and complicated operation in addition.
Flash method, owing to only pitch being carried out to flash distillation processing, lacks thermopolymerization, thus cause the toluene of product and quinoline insolubles lower.
Chinese patent CN 101775304 A disclose the preparation method of a kind of modified pitch and middle temperature modified pitch, the method is that coal tar is sent into after diamond heating, send into flash evaporator, after forming mid-temperature pitch, distillation enters reaction tower, reacting by heating in reaction tower, the pitch generating directly enters collection tower, makes middle temperature modified pitch; In reaction tower, send into part pitch to upgrading tower, under condition of negative pressure, carry out flash distillation, after flash distillation finishes, enter collection tower, make modified pitch.The method adopts the technique of flash distillation after first reaction, and pitch is processed and reacted without flash distillation, and in pitch, light constituent content is higher, causes in pitch reaction process secondary TI value lower, causes in modified pitch β resin content low, has influence on the quality of product; Meanwhile, because the steam output of light constituent in reaction process is larger, take away heat many, consumption of energy increases.
Chinese patent CN 1256406C discloses temperature and Production Process for Modified Pitch in single kettle type at a kind of intermittence, and this technique once completes the production of middle temperature and modified pitch in single still.First coal tar is proceeded in reactor to thermal dehydration.After dehydration finishes, continue intensification extraction mixed triolein and carbolineum, residue makes mid-temperature pitch through cooling process.Mid-temperature pitch is continued to reacting by heating, produce modified pitch.In production process, adopt coal gas as thermal source.The subject matter of this technique is that the oil quality of extraction is undesirable, and owing to adopting batch technology, throughput is limited; Its whole technological processs all complete in a reactor, and the heating material time is long, meanwhile, owing to adopting coal gas open firing, easily cause coking in reactor, affect work-ing life and the heat-transfer effect of equipment, and the energy and power consumption are significantly increased.
Summary of the invention
The purpose of this utility model is to provide the production system of a kind of efficient, energy-conservation, low-loss, free of contamination modified pitch.
The production system of modified pitch of the present utility model is achieved in the following ways.
The production system of modified pitch of the present utility model, comprises upgrading intermediate pitch processing units and asphalt modifier conversion unit with flash oil Flash Gas Compression Skid System, it is characterized in that:
The described upgrading intermediate asphalt production equipment with flash oil Flash Gas Compression Skid System comprises the vacuum flasher being connected with the second evaporator of tar processing unit (plant) by pipeline, by the pipeline heavy oil water cooler that the flash distillation oil gas vent at vacuum flasher top is connected therewith, by the pipeline heavy fuel separator that heavy oil water cooler is connected therewith, by the pipeline heavy oil sealed can that heavy fuel separator bottom is connected therewith, this heavy oil sealed can is connected with heavy oil storage tank by pipeline, the vacuum cooler-condenser being connected with the top of described heavy fuel separator by pipeline, by the pipeline vacuum tank that vacuum cooler-condenser bottom is connected therewith, by the pipeline vacuum pump that the top of vacuum tank is connected therewith, the bottom of described vacuum tank is connected with sump tank,
Described vacuum flasher, comprise housing, be located at flash distillation oil gas discharge port and the liquidometer Link Port of this case top, be located at the opening for feed of described housing one middle side part, described opening for feed is connected with the second evaporator mid-temperature pitch outlet of tar processing unit (plant) by pipeline, be located at the thermometer of this opening for feed below, be located at the manhole of described housing opposite side, be located at the pressure balance mouth of this manhole below, be located at the upgrading intermediate pitch outlet of described lower housing portion, described flash distillation oil gas vent is connected with heavy oil water cooler, insert in described housing one end, the feed-pipe that the other end is connected with described opening for feed, described feed-pipe is the feed-pipe lengthening, the length of its feed-pipe is 4/5 of diameter of the housing, and be provided with streams outlet in the bottom of described feed-pipe, be provided with the circular distribution device being connected with described inner walls in the bottom of described feed-pipe,
Described circular distribution device is by annular downtake cohort, and the annular riser cohort of annular downtake cohort alternative arrangement setting forms therewith;
Described asphalt modifier conversion unit comprises asphalt exchanger, the bituminous seal tank being connected with asphalt exchanger, with the tank connected bitumenpump of bituminous seal, and the upgrading reactor being connected with bitumenpump, the asphalt exchanger being connected with upgrading reactor and the hot melt salt heating system being connected with upgrading reactor and asphalt exchanger;
Described hot melt salt heating system is by hot molten salt furnace, one end is connected with hot melt salt furnace discharge mouth by pipeline, the hot melt salt pump that the other end is connected with the hot melt salt opening for feed on asphalt heater, one end is connected with the hot melt salt discharge port on asphalt heater, and the other end forms with the transport pipe that hot molten salt furnace opening for feed is connected;
In described asphalt exchanger, be respectively equipped with by pipeline and export with the upgrading intermediate pitch of vacuum flasher the upgrading intermediate bitumen feed mouth being connected, upgrading intermediate pitch discharge port after heat exchange, coal tar mouth and asphalt exchanger coal tar discharge port that the transfer lime of the coal tar heating with the Tar tube furnace from tar system of processing is connected;
The opening for feed of described bituminous seal tank is connected with the upgrading intermediate pitch discharge port of asphalt exchanger by pipeline, the discharge port of described bituminous seal tank is connected with bitumenpump opening for feed by pipeline, and the discharge port of described bitumenpump is connected with the upgrading intermediate bitumen feed mouth of asphalt heater by pipeline;
On described asphalt heater, be provided with the hot melt salt opening for feed and the heat exchange after heat fused salt discharge port that are connected with hot melt salt heating system;
Described upgrading reactor is by the housing with hot melt salt medium chuck, be arranged on material inlet and the bitumen flue gas discharge outlet on housing top, be arranged on the whipping appts in housing, be arranged on the material outlet of lower housing portion, described hot melt salt medium chuck is semi-canal type hot melt salt medium chuck, be provided with hot melt salt opening for feed in the bottom of hot melt salt medium chuck, be provided with heat exchange after heat fused salt discharge port on the top of hot melt salt medium chuck, described hot melt salt opening for feed is also connected with hot melt salt pump by pipeline, described hot melt salt discharge port is also connected with hot molten salt furnace by pipeline, make the hot melt salt under melt-flow state form closed circuit circulatory system in the hot melt salt medium chuck of upgrading reactor,
The material inlet of described upgrading reactor is connected with the upgrading intermediate pitch discharge port of asphalt heater by pipeline; The material outlet of described upgrading reactor is connected with modified pitch shaped device with bitumenpump by pipeline, and described bitumen flue gas discharge outlet is connected with washing device.
Described whipping appts is by the agitator motor and the step-down gear that are arranged on the case top of hot melt salt medium chuck, the stirring rake that step-down gear connects therewith, and the nonmetal scraper plate that is arranged on stirring rake outside forms.
Described annular downtake cohort is by downtake, the strut member I that downtake connects therewith with form with the liquid sprinkling disc that downtake bottom is connected by strut member I, described downtake is 200～700, described liquid sprinkling disc is lower than 30～70mm bottom downtake.
Described annular riser cohort is by riser, the strut member II that riser connects therewith with form with the umbrella crown that riser top is connected by strut member II, described riser is 60～210, described umbrella crown is higher than riser top 30～70mm.
The utility model has the advantages that:
The utility model is owing to having adopted the second evaporator mode that directly gravity flow enter vacuum flasher of mid-temperature pitch from tar processing unit (plant), make full use of the feature that mid-temperature pitch self temperature is high, enthalpy is large, mid-temperature pitch does not need external heat source can obtain the satisfactory upgrading intermediate pitch for the production of modified pitch carry out flash distillation under negative pressure state time.In flash vaporization process, have a small amount of thermosteresis, by interchanger heat exchange temperature raising, then through asphalt heater after fused salt heating, just can reach the temperature that upgrading intermediate pitch carries out upgrading reaction, reduced power and energy consumption.From the second evaporator of tar processing unit (plant), to bitumenpump, the conveying of pitch relies on the gravity flow of equipment potential difference to carry, and has saved power consumption.
Simultaneously, in the upgrading step of reaction of upgrading intermediate pitch, the utility model has adopted the heat source of hot melt salt as upgrading intermediate pitch and asphalt heater in transformation of the way reactor, has well solved the coking problem that upgrading material in reactor is heated inequality and brings thus.Because the specific heat capacity of fused salt is larger, be convenient to the insulation operation of upgrading intermediate pitch polymerization process, make the reaction process of upgrading intermediate pitch polymerization more steady, the quality index of the modified pitch of generation is more stable.Before polymerization, mid-temperature pitch first carries out flash distillation processing, has improved in mid-temperature pitch the content of secondary TI in TI value, QI value and reaction process, makes TI value in product, QI value and β resin content reach more preferably index.The top of while upgrading reactor is provided with bitumen flue gas discharge outlet and is connected with washing device, has ensured that whole reaction process does not have pollutent to leak.
Brief description of the drawings
Fig. 1 is the production system schematic diagram of modified pitch of the present utility model.
Fig. 2 is the utility model vacuum flasher structural representation.
Fig. 3 is the structural representation of the utility model vacuum flasher A part.
Fig. 4 is the utility model upgrading reactor structural representation.
Fig. 5 is the schematic diagram of another embodiment of production system of modified pitch of the present utility model.
Embodiment
Below in conjunction with brief description of the drawings embodiment of the present utility model.
As Figure 1-Figure 4, the production system of modified pitch of the present utility model, comprise upgrading intermediate pitch processing units, asphalt modifier conversion unit and the upgrading intermediate asphalt delivery pipeline 17 that is connected upgrading intermediate pitch processing units and asphalt modifier conversion unit, is characterized in that:
Described upgrading intermediate pitch processing units comprises the vacuum flasher 1 being connected with the second evaporator of tar processing unit (plant) by pipeline 16, by the pipeline heavy oil water cooler 2 that the flash distillation oil gas vent at vacuum flasher 1 top is connected therewith, by the pipeline heavy fuel separator 3 that heavy oil water cooler 2 is connected therewith, by the pipeline heavy oil sealed can 4 that heavy fuel separator 3 bottoms are connected therewith, this heavy oil sealed can 4 is connected with heavy oil storage tank by pipeline, the vacuum cooler-condenser 5 being connected with the top of described heavy fuel separator 3 by pipeline, by the pipeline vacuum tank 6 that vacuum cooler-condenser 5 bottoms are connected therewith, by the pipeline vacuum pump 7 that the top of vacuum tank 6 is connected therewith, the bottom of described vacuum tank 6 is connected with sump tank, in figure, 15 is heat-eliminating medium transport pipe.
As shown in Figure 3, vacuum flasher 1 described in the utility model, comprise housing 1-1, be located at flash distillation oil gas vent 1-10 and the liquidometer Link Port 1-11 at this housing 1-1 top, be located at the opening for feed 1-7 of described housing one middle side part, described opening for feed 1-7 is connected with the second evaporator discharge port of tar processing unit (plant) by pipeline 16, be located at the thermometer 1-6 of this opening for feed 1-7 below, be located at the manhole 1-2 of described housing 1-1 opposite side, be located at the pressure balance mouth 1-4 of this manhole 1-2 below, be located at the upgrading intermediate pitch discharge port 1-5 of described housing 1-1 bottom, described flash distillation oil gas discharge port 1-10 is connected with heavy oil water cooler 2, insert in described housing 1-1 one end, the feed-pipe 1-8 that the other end is connected with described opening for feed 1-7, described feed-pipe 1-8 is the feed-pipe lengthening, the length of its feed-pipe 1-8 is diameter of the housing 4/5, and be provided with streams outlet 1-9 in the bottom of described feed-pipe 1-8, be provided with the circular distribution device 1-3 being connected with described inner walls in the bottom of described feed-pipe 1-8,
Described circular distribution device 1-3 is by annular downtake cohort, and the annular riser cohort of annular downtake cohort alternative arrangement setting forms therewith;
Preferred described annular downtake cohort is by downtake 1-3-4, the strut member I 1-3-5 that downtake 1-3-4 connects therewith forms with the liquid sprinkling disc 1-3-6 being connected with downtake bottom by strut member I 1-3-5, described downtake 1-3-4 is 200～700, and described liquid sprinkling disc is lower than downtake bottom 30～70mm;
As shown in Figure 4, described annular riser cohort is by riser 1-3-3, the strut member II 1-3-2 that riser 1-3-3 connects therewith forms with the umbrella crown 1-3-1 being connected with riser top by strut member II 1-3-2, described riser 1-3-3 is 60～210, and described umbrella crown 1-3-1 is higher than riser top 30～70mm.
Asphalt modifier conversion unit described in the utility model comprises asphalt exchanger 8, the bituminous seal tank 9 being connected with asphalt exchanger 8, the bitumenpump 12 being connected with bituminous seal tank 9, and the upgrading reactor 10 being connected with bitumenpump 12, the asphalt exchanger 11 being connected with upgrading reactor 10 and the hot melt salt heating system being connected with upgrading reactor 10 and asphalt exchanger 11;
Described hot melt salt heating system is by hot molten salt furnace 14, one end is connected with hot molten salt furnace 14 discharge ports by pipeline, the hot melt salt pump 13 that the other end is connected with the hot melt salt opening for feed on asphalt heater 11, one end is connected with the heat exchange after heat fused salt discharge port on asphalt heater 11, and the other end forms with the transport pipe that hot molten salt furnace 14 opening for feeds are connected;
In described asphalt exchanger 8, be respectively equipped with the upgrading intermediate bitumen feed mouth 8-2 being connected with the upgrading intermediate pitch discharge port 1-5 of vacuum flasher 1 by upgrading intermediate asphalt delivery pipeline 17, upgrading intermediate pitch discharge port 8-1 after heating, coal tar mouth 8-3 and interchanger air outlet 8-4 that the transfer lime 8-5 of the coal tar heating with the Tar tube furnace from tar system of processing is connected;
The opening for feed of described bituminous seal tank 9 is connected with the upgrading intermediate pitch discharge port 8-1 after heating in asphalt exchanger 8 by pipeline, and the discharge port of described bituminous seal tank 9 is connected with the opening for feed of bitumenpump 12 by pipeline;
On described asphalt heater 11, be provided with the hot melt salt opening for feed and the heat exchange after heat fused salt discharge port that are connected with hot melt salt heating system;
As shown in Figure 5, upgrading reactor 10 described in the utility model is by the housing 10-1 with hot melt salt medium chuck 10-4, be arranged on material inlet 10-10 and the bitumen flue gas discharge outlet 10-8 on housing 10-1 top, be arranged on the whipping appts in housing 10-1, be arranged on the material outlet 10-6 of housing 10-1 bottom, described hot melt salt medium chuck 10-4 is semi-canal type hot melt salt medium chuck, the hot melt salt opening for feed 10-5 being provided with in hot melt salt medium chuck 10-4 bottom, at the upgrading reactor hot melt salt discharge port 10-7 after heat exchange that is provided with on hot melt salt medium chuck 10-4 top, described hot melt salt opening for feed 10-5 is also connected with hot melt salt pump 13 by pipeline, upgrading reactor hot melt salt discharge port 10-7 is also connected with hot molten salt furnace 14 by pipeline, make the hot melt salt under melt-flow state form closed circuit circulatory system in the hot melt salt medium chuck 10-4 of upgrading reactor 10, can ensure the material homogeneous heating in upgrading reactor, whipping appts and kettle contact site adopt mechanical seal.
As shown in Figure 4, the material inlet 10-10 of upgrading reactor 10 described in the utility model is connected with the discharge port of asphalt heater 11 by pipeline; The material outlet 10-7 of described upgrading reactor 10 is connected with modified pitch shaped device 15 with bitumenpump 12 by pipeline, and described bitumen flue gas discharge outlet 10-8 is connected with washing device, has ensured that whole reaction process does not have pollutent to leak.
Whipping appts described in the utility model is by the agitator motor and the step-down gear 10-9 that are arranged on the case top of hot melt salt medium chuck, the stirring rake 10-2 that agitator motor and step-down gear 10-9 connect therewith, the nonmetal scraper plate 10-3 in the stirring rake 10-2 being arranged on outside forms.Its nonmetal scraper plate 10-3 contacts with the still wall of upgrading reactor 10, the pitch adhering to can be scraped, to avoid being heated for a long time coking on still wall.
The utility model is also provided with the transport pipe being connected with hard-pitch forming device 18 on described upgrading intermediate asphalt delivery pipeline 17.
Number in the figure 19 is heat-eliminating medium inlet/outlet pipe.
Adopt the preparation system of modified pitch of the present utility model to produce modified pitch, mid-temperature pitch from tar processing unit (plant) second evaporator is sent into the upgrading intermediate pitch processing units with flash oil Flash Gas Compression Skid System by pipeline, flash distillation oil gas after vacuum flasher flash distillation is fed to heavy oil treatment facility and carry out heavy oil fraction, separation and condensation recycling, and the upgrading intermediate pitch after flash distillation is sent into asphalt modifier conversion unit and produce modified pitch, concrete steps are as follows:
1) first start vacuum pump, vacuum flasher 1 is vacuumized, the vacuum keep that makes vacuum flasher 1 is at-20Kpa～-5Kpa;
2) the mid-temperature pitch gravity flow that is 360 DEG C～370 DEG C from the temperature of second evaporator enters in vacuum flasher 1, is evenly discharged on circular distribution device, and flows and be covered with circular distribution device surface rapidly by the streams outlet 1-9 on feed-pipe 1-8;
3) mid-temperature pitch is uniformly distributed on the circular distribution device of vacuum flasher, and flow out downwards by the downtake 1-3-4 on circular distribution device, drop on the upper further dispersion of liquid sprinkling disc 1-3-6, be radial flowing down downwards at liquid sprinkling disc 1-3-6 Shang Zi center, make mid-temperature pitch thickness of liquid film at 1～2mm; Carbolineum in mid-temperature pitch and heavy washing oil evaporate rapidly, overflow by the riser 1-3-3 on circular distribution device, and enter in heavy oil water cooler 2 through the flash distillation oil gas vent 1-10 at vacuum flasher top, the flash-off time of mid-temperature pitch in flasher 1 is 3～20min;
4) flash distillation oil gas is cooled to 80～100 DEG C in heavy oil water cooler 2 becomes heavy oil fraction, enters in heavy fuel separator 3, carries out gas-liquid separation;
5) the interior isolated heavy oil fraction of heavy fuel separator 3 enters heavy oil sealed can 4, and the heavy oil fraction in this heavy oil sealed can 4 is delivered to heavy oil storage tank by pipeline;
6) the isolated noncondensable gas of heavy fuel separator 4 enters vacuum cooler-condenser 5 by pipeline, is cooled to 30 DEG C～40 DEG C in vacuum cooler-condenser 5, and cooled noncondensable gas enters in vacuum tank 6 by pipeline;
7) noncondensable gas in vacuum tank 6 is delivered to vent gas washing system washing through vacuum pump 7, and the noncondensable gas after washing is delivered to tube furnace burning;
8) the upgrading intermediate pitch gravity flow generating after flash distillation enters asphalt exchanger 8, in asphalt exchanger 8, with coal tar heat exchange temperature raising to 340 from tar system of processing Tar tube furnace heating DEG C～380 DEG C, bituminous seal tank 9 is sent in the upgrading intermediate pitch gravity flow after temperature raising;
10) start pump for liquid salts 13, send into more than 500 DEG C hot melt salt by pipeline toward asphalt heater 11;
11) the upgrading intermediate pitch that bitumenpump 12 is extracted out from bituminous seal tank 9 tops is sent into asphalt heater 11, enter upgrading intermediate pitch in asphalt heater 11 after hot melt salt heating temperature raising to 380 DEG C～450 DEG C, enter in upgrading reactor 10, starting the upgrading intermediate pitch of whipping appts after to temperature raising stirs, make upgrading intermediate pitch in upgrading reactor 10, carry out heat polymerization, reaction times is 3～8 hours, pump for liquid salts also passes into more than 500 DEG C hot melt salt in the chuck of upgrading reactor simultaneously, the thermal barrier being incubated as upgrading upgrading reactor 10, the nonmetal scraper plate 10-3 that the stirring arm 10-2 side of whipping appts arranges scrapes the pitch adhering on still wall,
12) after reaction finishes, the softening temperature of modified pitch is (mercury process) 105～125 DEG C, toluene insolubles content 32～36%, quinoline insolubles content 9～14%, β resin content is greater than 24%, coking value 54～65%, ash content is less than 0.3%, moisture is less than 1%, starts bitumenpump and send modified pitch shaped device 15 by the qualified modified pitch in upgrading reactor, packaging warehouse-in.
Example 1:
The preparation method of a kind of modified pitch of the present utility model, it is characterized in that: the mid-temperature pitch from tar processing unit (plant) second evaporator is sent into the upgrading intermediate pitch processing units with flash oil Flash Gas Compression Skid System by pipeline, flash distillation oil gas after vacuum flasher flash distillation is fed to heavy oil treatment facility and carry out heavy oil fraction, separation and condensation recycling, and the upgrading intermediate pitch after flash distillation is sent into asphalt modifier conversion unit and produce modified pitch, concrete steps are as follows:
First start vacuum pump, vacuum flasher 1 is vacuumized, make the vacuum tightness of vacuum flasher 1 at-10 Kpa～-5Kpa; The mid-temperature pitch gravity flow that is 360 DEG C 370 DEG C from second evaporator, temperature enters in vacuum flasher 1, evenly be discharged on circular distribution device by the outlet 1-9 on feed-pipe, and flow out downwards by the downtake 1-3-4 on circular distribution device, drop on to spatter on liquid 1-3-6 dish and further disperse, make asphaltic liquid film thickness at 1～2mm, the light constituents such as the heavy washing oil in mid-temperature pitch evaporate rapidly, by riser, 1-3-3 overflows, flash distillation oil gas vent 1-10 through vacuum flasher 1 top enters in heavy oil water cooler 2, and flash-off time is 8min; Flash distillation oil gas is cooled to 90 DEG C in heavy oil water cooler 2 becomes heavy oil fraction, enters in heavy fuel separator 3, carries out gas-liquid separation; The interior isolated heavy oil fraction of heavy fuel separator 3 enters heavy oil sealed can 4, and the heavy oil fraction in this heavy oil sealed can 4 is delivered to heavy oil storage tank by pipeline; The isolated noncondensable gas of heavy fuel separator 3 enters vacuum cooler-condenser 5 by pipeline, is cooled to 30 DEG C in vacuum cooler-condenser 5, and cooled noncondensable gas enters in vacuum tank 6 by pipeline; Noncondensable gas in vacuum tank 6 is through vacuum pumping to vent gas washing system washing, and the noncondensable gas after washing is delivered to tube furnace burning; The upgrading intermediate pitch gravity flow generating after flash distillation enters in asphalt exchanger 8, and with the coal tar heat exchange temperature raising to 340 DEG C from the heating of tar system of processing Tar tube furnace, bituminous seal tank 9 is sent in the upgrading intermediate pitch gravity flow after preheating; Start pump for liquid salts, send into more than 500 DEG C hot melt salt by pipeline toward asphalt heater 11; The upgrading intermediate pitch that bitumenpump 12 is extracted out from bituminous seal tank 9 tops is sent into asphalt heater 11, the upgrading intermediate pitch entering in asphalt heater 11 heats temperature raising to 380 DEG C through hot melt salt, enter in upgrading reactor 10, starting stirring rake stirs upgrading intermediate pitch, make upgrading intermediate pitch carry out heat polymerization at upgrading reactor 10, reaction times is 3 hours, and the nonmetal scraper plate 10-3 of stirring arm side scrapes the pitch adhering on upgrading reactor still wall simultaneously; After reaction finishes, start bitumenpump 12 and send modified pitch formation system by the qualified modified pitch in upgrading reactor 10, packaging warehouse-in;
The softening temperature of modified pitch is (mercury process) 106 DEG C, toluene insolubles content 32%, quinoline insolubles content 9%, β resin content is greater than 24%, coking value 55%, ash content 0.28%, moisture 0.9%, start bitumenpump and send modified pitch formation system by the qualified modified pitch in upgrading reactor, packaging warehouse-in after moulding.
Example 2:
The preparation method of a kind of modified pitch of the present utility model, that the mid-temperature pitch from tar processing unit (plant) second evaporator is sent into the upgrading intermediate pitch processing units with flash oil Flash Gas Compression Skid System by pipeline, flash distillation oil gas after vacuum flasher flash distillation is fed to heavy oil treatment facility and carry out heavy oil fraction, separate and condensation recycling, and using the upgrading intermediate pitch one side after flash distillation as upgrading intermediate pitch, send into asphalt modifier conversion unit by upgrading intermediate asphalt delivery pipe and produce modified pitch, on the other hand as hard pitch the finished product, directly deliver to hard-pitch forming device by hard pitch transfer line, concrete steps are as follows:
First start vacuum pump, vacuum flasher 1 is vacuumized, the vacuum tightness that makes vacuum flasher 1 is at-15Kpa～-10Kpa; The mid-temperature pitch gravity flow that is 360 DEG C～370 DEG C from second evaporator, temperature enters in vacuum flasher 1, evenly be discharged on circular distribution device by the outlet 1-9 on feed-pipe, and flow out downwards by the downtake 1-3-4 on circular distribution device, drop on the upper further dispersion of liquid sprinkling disc 1-3-6, make asphaltic liquid film thickness at 1～2mm, the light constituents such as the carbolineum in mid-temperature pitch evaporate rapidly, by riser, 1-3-3 overflows, flash distillation oil gas vent 1-10 through vacuum flasher top enters in heavy oil water cooler 2, and flash-off time is 13min;
Flash distillation oil gas is cooled to 90 DEG C in heavy oil water cooler 2 becomes heavy oil fraction, enters in heavy fuel separator 3, carries out gas-liquid separation; The interior isolated heavy oil fraction of heavy fuel separator 3 enters heavy oil sealed can 4, and the heavy oil fraction in this heavy oil sealed can 4 is delivered to heavy oil storage tank by pipeline; The isolated noncondensable gas of heavy fuel separator 4 enters vacuum cooler-condenser 5 by pipeline, is cooled to 30 DEG C in vacuum cooler-condenser 5, and cooled noncondensable gas enters in vacuum tank 6 by pipeline; Noncondensable gas in vacuum tank 6 is through vacuum pumping to vent gas washing system washing, and the noncondensable gas after washing is delivered to tube furnace burning;
As upgrading intermediate pitch, gravity flow enters in asphalt exchanger 8 on upgrading intermediate pitch one tunnel generating after flash distillation, with the coal tar heat exchange temperature raising to 340 DEG C from the heating of tar system of processing Tar tube furnace, bituminous seal tank 9 is sent in the upgrading intermediate pitch gravity flow after preheating; Start pump for liquid salts, send into more than 500 DEG C hot melt salt by pipeline toward asphalt heater 11; The upgrading intermediate pitch that bitumenpump 12 is extracted out from bituminous seal tank 9 tops is sent into asphalt heater 11, the upgrading intermediate pitch entering in asphalt heater 11 heats temperature raising to 380 DEG C through hot melt salt, enter in upgrading reactor 10, starting stirring rake stirs upgrading intermediate pitch, make upgrading intermediate pitch carry out heat polymerization at upgrading reactor 10, reaction times is 5 hours, and the nonmetal scraper plate 10-3 of stirring arm side scrapes the pitch adhering on upgrading reactor still wall simultaneously; After reaction finishes, start bitumenpump 12 and send modified pitch formation system by the qualified modified pitch in upgrading reactor 10, packaging warehouse-in;
The softening temperature (mercury process) of the modified pitch of producing is 107 DEG C, toluene insolubles content 34%, and quinoline insolubles content 9.5%, β resin content 24%, coking value 56%, ash content is less than 0.25%, and moisture is less than 0.8%.
Hard-pitch forming device 18, as hard pitch the finished product, is directly delivered to by hard pitch transfer line in another road of upgrading intermediate pitch generating after flash distillation.As shown in Figure 5.
This method is coproduction hard pitch and modified pitch simultaneously.
The utility model is rational in infrastructure, and efficient energy-saving has significantly promoted the indices of pitch, has greatly reduced energy and power engineering consumption, has ensured that whole reaction process does not have pollutent to leak.
Claims (5)
1. a production system for modified pitch, comprises upgrading intermediate pitch processing units, and asphalt modifier conversion unit and the upgrading intermediate asphalt delivery pipeline that is connected upgrading intermediate pitch processing units and asphalt modifier conversion unit, is characterized in that:
Described upgrading intermediate pitch processing units comprises the vacuum flasher being connected with the second evaporator of tar processing unit (plant) by pipeline, by the pipeline heavy oil water cooler that the flash distillation oil gas vent at vacuum flasher top is connected therewith, by the pipeline heavy fuel separator that heavy oil water cooler is connected therewith, by the pipeline heavy oil sealed can that heavy fuel separator bottom is connected therewith, this heavy oil sealed can is connected with heavy oil storage tank by pipeline, the vacuum cooler-condenser being connected with the top of described heavy fuel separator by pipeline, by the pipeline vacuum tank that vacuum cooler-condenser bottom is connected therewith, by the pipeline vacuum pump that the top of vacuum tank is connected therewith, the bottom of described vacuum tank is connected with sump tank,
Described vacuum flasher, comprise housing, be located at flash distillation oil gas discharge port and the liquidometer Link Port of this case top, be located at the opening for feed of described housing one middle side part, described opening for feed is connected with the second evaporator discharge port of tar processing unit (plant), be located at the thermometer of this opening for feed below, be located at the manhole of described housing opposite side, be located at the pressure balance mouth of this manhole below, be located at the upgrading intermediate pitch discharge port of described lower housing portion, described flash distillation oil gas discharge port is connected with heavy oil water cooler, insert in described housing one end, the feed-pipe that the other end is connected with described opening for feed, described feed-pipe is the feed-pipe lengthening, the length of its feed-pipe is 4/5 of diameter of the housing, and be provided with streams outlet in the bottom of described feed-pipe, be provided with the circular distribution device being connected with described inner walls in the bottom of described feed-pipe,
Described circular distribution device is by annular downtake cohort, and the annular riser cohort of annular downtake cohort alternative arrangement setting forms therewith;
Described asphalt modifier conversion unit comprises asphalt exchanger, the bituminous seal tank being connected with asphalt exchanger, with the tank connected bitumenpump of bituminous seal, and the upgrading reactor being connected with bitumenpump, the asphalt exchanger being connected with upgrading reactor and the hot melt salt heating system being connected with upgrading reactor and asphalt exchanger;
Described hot melt salt heating system is by hot molten salt furnace, one end is connected with hot melt salt furnace discharge mouth by pipeline, the hot melt salt pump that the other end is connected with the hot melt salt opening for feed on asphalt heater, one end is connected with the heat exchange after heat fused salt discharge port on asphalt heater, and the other end forms with the transport pipe that hot molten salt furnace opening for feed is connected;
In described asphalt exchanger, be respectively equipped with by upgrading intermediate asphalt delivery pipeline and vacuum flasher
The upgrading intermediate bitumen feed mouth that upgrading intermediate pitch discharge port connects, upgrading intermediate pitch discharge port after heating, coal tar mouth and asphalt exchanger coal tar discharge port that the transfer lime of the coal tar heating with the Tar tube furnace from tar system of processing is connected;
The opening for feed of described bituminous seal tank is connected with the upgrading intermediate pitch discharge port in asphalt exchanger by pipeline, and the discharge port of described bituminous seal tank is connected with the opening for feed of bitumenpump by pipeline;
On described asphalt heater, be provided with the hot melt salt opening for feed and the heat exchange after heat fused salt discharge port that are connected with hot melt salt heating system,
Described upgrading reactor is by the housing with hot melt salt medium chuck, be arranged on material inlet and the bitumen flue gas discharge outlet on housing top, be arranged on the whipping appts in housing, be arranged on the material outlet of lower housing portion, described hot melt salt medium chuck is semi-canal type hot melt salt medium chuck, be provided with hot melt salt opening for feed in the bottom of hot melt salt medium chuck, be provided with the upgrading reactor hot melt salt discharge port after heat exchange on the top of hot melt salt medium chuck, described hot melt salt opening for feed is also connected with hot melt salt pump by pipeline, upgrading reactor hot melt salt discharge port is also connected with hot molten salt furnace by pipeline, make the hot melt salt under melt-flow state form closed circuit circulatory system in the hot melt salt medium chuck of upgrading reactor,
The material inlet of described upgrading reactor is connected with the discharge port of asphalt heater by pipeline; The material outlet of described upgrading reactor is connected with modified pitch shaped device with bitumenpump by pipeline, and described bitumen flue gas discharge outlet is connected with washing device.
2. the production system of modified pitch according to claim 1, it is characterized in that described whipping appts is by the agitator motor and the step-down gear that are arranged on the case top of hot melt salt medium chuck, the stirring rake that step-down gear connects therewith, the nonmetal scraper plate that is arranged on stirring rake outside forms.
3. according to the production system of claim 1 modified pitch, it is characterized in that described annular downtake cohort is by downtake, therewith downtake connect strut member I with form with the liquid sprinkling disc that downtake bottom is connected by strut member I, described downtake is 200～700, and described liquid sprinkling disc is lower than downtake bottom 30～70mm.
4. the production system of modified pitch according to claim 1, it is characterized in that described annular riser cohort is by riser, therewith riser connect strut member II with form with the umbrella crown that riser top is connected by strut member II, described riser is 60～210, and described umbrella crown is higher than riser top 30～70mm.
5. the production system of modified pitch according to claim 1, is characterized in that being also provided with the transport pipe being connected with hard-pitch forming device on described upgrading intermediate asphalt delivery pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420039252.0U CN203741272U (en) | 2014-01-22 | 2014-01-22 | Production system of modified pitch |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420039252.0U CN203741272U (en) | 2014-01-22 | 2014-01-22 | Production system of modified pitch |
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| CN203741272U true CN203741272U (en) | 2014-07-30 |
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| CN201420039252.0U Withdrawn - After Issue CN203741272U (en) | 2014-01-22 | 2014-01-22 | Production system of modified pitch |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103756704A (en) * | 2014-01-22 | 2014-04-30 | 鞍山兴德工程技术有限公司 | System for producing modified coal tar pitch and preparation method thereof |
| CN104531192A (en) * | 2014-12-11 | 2015-04-22 | 山东钢铁股份有限公司 | Alternative-operation control device and process of tubular furnace |
| CN105199766A (en) * | 2015-10-22 | 2015-12-30 | 鞍山兴德材料科技股份有限公司 | Preparation method of mesophase pitch coke raw material for power lithium battery cathode material |
-
2014
- 2014-01-22 CN CN201420039252.0U patent/CN203741272U/en not_active Withdrawn - After Issue
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103756704A (en) * | 2014-01-22 | 2014-04-30 | 鞍山兴德工程技术有限公司 | System for producing modified coal tar pitch and preparation method thereof |
| CN103756704B (en) * | 2014-01-22 | 2015-03-11 | 鞍山兴德工程技术有限公司 | System for producing modified coal tar pitch and preparation method thereof |
| CN104531192A (en) * | 2014-12-11 | 2015-04-22 | 山东钢铁股份有限公司 | Alternative-operation control device and process of tubular furnace |
| CN105199766A (en) * | 2015-10-22 | 2015-12-30 | 鞍山兴德材料科技股份有限公司 | Preparation method of mesophase pitch coke raw material for power lithium battery cathode material |
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