CN102267868A - Industrial production apparatus for trichloroethylene - Google Patents
Industrial production apparatus for trichloroethylene Download PDFInfo
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- CN102267868A CN102267868A CN2010101884552A CN201010188455A CN102267868A CN 102267868 A CN102267868 A CN 102267868A CN 2010101884552 A CN2010101884552 A CN 2010101884552A CN 201010188455 A CN201010188455 A CN 201010188455A CN 102267868 A CN102267868 A CN 102267868A
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Abstract
The invention provides an industrial production apparatus for trichloroethylene. The apparatus is characterized in that: an acetylene air inlet pipeline and a chlorine gas air inlet pipeline are respectively connected with an inlet end of a chlorination tower; an outlet end of a crude tetrachloroethane tank is connected with an inlet of a tetrachloroethane tower; an outlet end of a material feeding preheater of a dehydrochlorination reactor is connected with an inlet end of a desorber; an outlet end of a desorption residue tank is connected with an inlet end of a low-boiler tower; an outlet end arranged on the lower portion of the low-boiler tower is respectively connected with an inlet end of a reboiler of the low-boiler tower and an inlet end of a trichloroethylene tower; an outlet end of a trichloroethylene residue tank is connected with an inlet end of a middle distillate tower; an outlet end arranged on the lower portion of the middle distillate tower is respectively connected with an inlet end of a reboiler of the middle distillate tower and an inlet end of a tetrachloroethylene tower; heat exchanging devices of each complete condenser and each end cooler adopt graphite parts dipped in modified phenol formaldehyde resin. The industrial production apparatus for the trichloroethylene has characteristics of reasonable structure, large production capacity, safe, stable and long-period operation, and the prepared trichloroethylene has high quality.
Description
Technical field
The invention provides a kind of improved trieline production equipment.
Background technology
At present, domestic trieline manufacturing enterprise's overwhelming majority employing " gas phase catalysis dehydrochlorination method " is produced.Its simple production flow process is: chlorine, acetylene gas generate thick tetrachloroethane in the chlorination tower, thick tetrachloroethane is vaporized after rectifying, dehydrochlorination generates trieline in the dehydrochlorination reaction device, passes through a series of distillation operation then, produces qualified trieline product.Because " gas phase catalysis dehydrochlorination method " trieline production equipment is emerging in recent years production technique, in the process of domestic other trieline manufacturing enterprise operations, a series of defective and problem have all appearred, show that plant capacity is less than normal, be about 1.0 ten thousand tons/year, energy consumption is higher; The unit equipment load is less; The heat comprehensive utilization of production equipment is relatively poor; The dielectric corrosion problem of each operation of production equipment is difficult to solve; Trieline product second-rate.
Summary of the invention
Technical problem to be solved by this invention is, a kind of trieline industrial production device is provided, and this plant capacity is big, can be safely, stablize long-term operation.
The present invention realizes like this, the trieline industrial production device, it has the acetylene admission line to link to each other with chlorination tower entrance end respectively with the chlorine admission line, chlorination tower exit end links to each other with chlorination tower complete condenser entrance end, chlorination tower complete condenser exit end links to each other with chlorination return tank entrance end and chlorination tower tail cooler entrance end respectively, chlorination tower tail cooler exit end links to each other with chlorination return tank entrance end and gas-liquid separator entrance end respectively, the gas-liquid separator exit end links to each other with the tail gas buffer entrance end, the tail gas buffer exit end links to each other with the hydraulic jet pump entrance end, the hydraulic jet pump exit end links to each other with chlorination tail tank entrance end, chlorination tail tank exit end links to each other with chlorination afterbay entrance end, chlorination afterbay exit end links to each other with the pressure pump entrance end, another entrance end of pressure pump exit end and hydraulic jet pump links to each other, chlorination return tank exit end links to each other with thick tetrachloroethane jar entrance end, thick tetrachloroethane jar exit end links to each other with tetrachloroethane tower entrance end, tetrachloroethane tower lower part outlet end links to each other with tetrachloroethane tower reboiler entrance end and smart tetrachloroethane jar entrance end respectively, tetrachloroethane tower reboiler exit end links to each other with another entrance end of tetrachloroethane tower, tetrachloroethane top of tower exit end links to each other with tetrachloroethane tower complete condenser entrance end, tetrachloroethane tower complete condenser exit end links to each other with tetrachloroethane tower return tank entrance end and tetrachloroethane tower tail cooler entrance end respectively, tetrachloroethane tail cooler exit end links to each other with tetrachloroethane tower return tank entrance end, smart tetrachloroethane jar exit end links to each other with tetrachloroethane vaporizer entrance end, tetrachloroethane vaporizer exit end links to each other with dehydrochlorination reaction device feed preheater entrance end, dehydrochlorination reaction device feed preheater exit end links to each other with thermal oil preheater entrance end, thermal oil preheater exit end links to each other with dehydrochlorination reaction device entrance end, dehydrochlorination reaction device exit end links to each other with another entrance end of dehydrochlorination reaction device feed preheater, another exit end of dehydrochlorination reaction device feed preheater links to each other with the desorption tower entrance end, desorption tower outlet at bottom end links to each other with the desorption tower reboiler entrance end, another entrance end of desorption tower reboiler exit end and desorption tower links to each other, desorption tower top exit end links to each other with desorption tower complete condenser entrance end, desorption tower complete condenser exit end links to each other with desorption tower return tank entrance end and Analytic Tower tail cooler entrance end respectively, Analytic Tower tail cooler exit end links to each other with desorption tower return tank entrance end, desorb return tank exit end links to each other with extraction-container flow container entrance end, extraction-container flow container exit end links to each other with the low tower entrance end that boils, the low tower lower part outlet end that boils links to each other with low tower reboiler entrance end and the trieline tower entrance end of boiling respectively, the low tower reboiler exit end that boils links to each other with low another entrance end of tower that boils, the low top of tower exit end that boils links to each other with the low tower complete condenser entrance end that boils, the low tower complete condenser exit end that boils reaches the low tower tail cooler entrance end that boils with the low tower return tank entrance end that boils respectively and links to each other, the low tower tail cooler exit end that boils links to each other with the low tower return tank entrance end that boils, trieline tower lower part outlet end links to each other with trieline tower reboiler entrance end and trieline still flow container entrance end respectively, trieline tower reboiler exit end links to each other with another entrance end of trieline tower, trieline tower top exit end links to each other with trieline tower complete condenser entrance end, trieline tower complete condenser exit end links to each other with trieline tower tail cooler entrance end and trieline tower return tank entrance end respectively, trieline tower tail cooler exit end links to each other with trieline return tank entrance end, trieline return tank exit end respectively with another entrance end of trieline tower, trieline discharging cooler inlet end links to each other, trieline still flow container exit end links to each other with middle runnings tower entrance end, middle runnings tower lower part outlet end links to each other with middle runnings tower reboiler entrance end and zellon tower entrance end respectively, middle runnings tower top exit end links to each other with middle runnings tower complete condenser entrance end, middle runnings tower complete condenser exit end links to each other with middle runnings tower tail cooler entrance end and middle runnings tower return tank entrance end respectively, middle runnings tower tail cooler exit end links to each other with another entrance end of middle runnings tower return tank, middle runnings tower return tank exit end links to each other with another entrance end of desorption tower still flow container, zellon tower lower part outlet end and zellon tower reboiler entrance end, zellon tower top exit end links to each other with zellon tower complete condenser entrance end, zellon tower complete condenser exit end links to each other with zellon tower return tank entrance end and zellon tail cooler entrance end respectively, zellon tail cooler exit end links to each other described each complete condenser with another entrance end of zellon tower return tank, the heat exchange device of each tail cooler adopts the graphite piece of modified phenolic resin impregnate with tallow.
Adopt the trieline industrial production device of said structure, rational in infrastructure, throughput is big, can be safely, stablize long-term operation.The trieline quality product height of being produced.
Description of drawings
Fig. 1 is the synoptic diagram of the part of structure of the present invention.
Fig. 2 is the synoptic diagram of another part of structure of the present invention.
Fig. 3 is the synoptic diagram of the acetylene gas dry decontamination apparatus structure among the present invention.
Fig. 4 is the synoptic diagram of the dehydrochlorination reaction apparatus structure among the present invention.
Fig. 5 is the synoptic diagram of the gas distributor structure among the present invention.
Fig. 6 is the A-A sectional view of Fig. 5.
Fig. 7 has represented the master, has propped up the assembly relation of distribution pipe.
Fig. 8 is the B-B sectional view of Fig. 5.
Embodiment
Further specify the present invention below in conjunction with accompanying drawing.
As shown in drawings, the present invention's trieline industrial production device, it has the acetylene admission line to link to each other with chlorination tower 9 entrance ends respectively with the chlorine admission line, chlorination tower 9 exit end link to each other with chlorination tower complete condenser 7 entrance ends, chlorination tower complete condenser 7 exit end link to each other with chlorination return tank 8 entrance ends and chlorination tower tail cooler 6 entrance ends respectively, chlorination tower tail cooler 6 exit end link to each other with chlorination return tank 8 entrance ends and gas-liquid separator 5 entrance ends respectively, gas-liquid separator 5 exit end link to each other with tail gas buffer 4 entrance ends, tail gas buffer 4 exit end link to each other with hydraulic jet pump 3 entrance ends, hydraulic jet pump 3 exit end link to each other with chlorination tail tank 10 entrance ends, chlorination tail tank 10 exit end link to each other with chlorination afterbay 1 entrance end, chlorination afterbay 1 exit end links to each other with pressure pump 2 entrance ends, pressure pump 2 exit end link to each other with hydraulic jet pump 3 another entrance ends, chlorination return tank 8 exit end link to each other with thick tetrachloroethane jar 11 entrance ends, thick tetrachloroethane jar 11 exit end link to each other with tetrachloroethane tower 12 entrance ends, tetrachloroethane tower 12 lower part outlet ends link to each other with tetrachloroethane tower reboiler 13 entrance ends and smart tetrachloroethane jar 17 entrance ends respectively, tetrachloroethane tower reboiler 13 exit end link to each other with another entrance end of tetrachloroethane tower 12, tetrachloroethane tower 12 top exit ends link to each other with tetrachloroethane tower complete condenser 14 entrance ends, tetrachloroethane tower complete condenser 14 exit end link to each other with tetrachloroethane tower return tank 16 entrance ends and tetrachloroethane tower tail cooler 15 entrance ends respectively, tetrachloroethane tail cooler 15 exit end link to each other with tetrachloroethane tower return tank 16 entrance ends, smart tetrachloroethane jar (17) exit end links to each other with tetrachloroethane vaporizer 18 entrance ends, tetrachloroethane vaporizer exit end links to each other with dehydrochlorination reaction device feed preheater 21 entrance ends, dehydrochlorination reaction device feed preheater 21 exit end link to each other with thermal oil preheater 19 entrance ends, thermal oil preheater 19 exit end link to each other with dehydrochlorination reaction device 20 entrance ends, dehydrochlorination reaction device 20 exit end link to each other with dehydrochlorination reaction device feed preheater 21 another entrance ends, dehydrochlorination reaction device feed preheater 21 another exit end link to each other with desorption tower 22 entrance ends, desorption tower 22 outlet at bottom ends link to each other with desorption tower reboiler (23) entrance end, desorption tower reboiler 23 exit end link to each other with desorption tower 22 another entrance ends, desorption tower top exit end links to each other with desorption tower complete condenser 24 entrance ends, desorption tower complete condenser exit end links to each other with desorption tower return tank 26 entrance ends and Analytic Tower tail cooler 25 entrance ends respectively, Analytic Tower tail cooler 25 exit end link to each other with desorption tower return tank 26 entrance ends, desorb return tank 26 exit end link to each other with extraction-container flow container 27 entrance ends, extraction-container flow container 27 exit end link to each other with low tower 28 entrance ends that boil, the low tower 28 lower part outlet ends that boil link to each other with low tower reboiler 29 entrance ends and trieline tower 33 entrance ends of boiling respectively, the low tower reboiler exit end that boils links to each other with low another entrance end of tower that boils, the low tower 28 top exit ends that boil link to each other with low tower complete condenser 30 entrance ends that boil, low tower complete condenser 30 exit end that boil reach low tower tail cooler 31 entrance ends that boil with low tower return tank 32 entrance ends that boil respectively and link to each other, low tower tail cooler 31 exit end that boil link to each other with low tower return tank 32 entrance ends that boil, trieline tower 33 lower part outlet ends link to each other with trieline tower reboiler 34 entrance ends and trieline still flow container 39 entrance ends respectively, trieline tower reboiler 34 exit end link to each other with trieline tower 33 another entrance ends, trieline tower 33 top exit end link to each other with trieline tower complete condenser 35 entrance ends, trieline tower complete condenser 35 exit end link to each other with trieline tower tail cooler 36 entrance ends and trieline tower return tank 37 entrance ends respectively, trieline tower tail cooler 36 exit end link to each other with trieline return tank 37 entrance ends, trieline return tank 37 exit end respectively with trieline tower 33 another entrance ends, trieline discharging water cooler 38 entrance ends link to each other, trieline still flow container 39 exit end link to each other with middle runnings tower 40 entrance ends, middle runnings tower 40 lower part outlet ends link to each other with middle runnings tower reboiler 41 entrance ends and zellon tower 45 entrance ends respectively, middle runnings tower 40 top exit end link to each other with middle runnings tower complete condenser 42 entrance ends, middle runnings tower complete condenser 42 exit end link to each other with middle runnings tower tail cooler 43 entrance ends and middle runnings tower return tank 44 entrance ends respectively, middle runnings tower tail cooler 43 exit end link to each other with middle runnings tower return tank 44 another entrance ends, middle runnings tower return tank 44 exit end link to each other with desorption tower still flow container 27 another entrance ends, zellon tower 45 lower part outlet ends and zellon tower reboiler 46 entrance ends, zellon tower 45 top exit end link to each other with zellon tower complete condenser 47 entrance ends, zellon tower complete condenser 47 exit end link to each other with zellon tower return tank 49 entrance ends and zellon tail cooler 48 entrance ends respectively, zellon tail cooler 48 exit end link to each other described each complete condenser with zellon tower return tank 49 another entrance ends, the heat exchange device of each tail cooler adopts the graphite piece of modified phenolic resin impregnate with tallow.The structure of the heat exchange device of each complete condenser, each tail cooler is identical with existing graphite material.
The concrete working process of the present invention's production equipment is, enter chlorination tower 9 from the acetylene of acetylene admission line with from the chlorine of chlorine admission line, after in containing the mother liquor of catalyzer, reacting, gas phase enters chlorination tower complete condenser 7, after the preliminary condensation of recirculated water, enter chlorination tower return tank 8, uncooled gas phase enters chlorination tower tail cooler 6, flow into chlorination tower return tank 8 through the condensed liquid phase of the chilled brine degree of depth, noncondensable gas is evacuated to gas-liquid separator 5 by vacuum, gas-liquid separator 5 isolated liquid phases enter thick tetrachloroethane jar 11, gas phase enters tail gas buffer 4, tail gas in the tail gas buffer enters hydraulic jet pump 3, utilize the change in flow of hydraulic jet pump to vacuumize, the water that comes out from hydraulic jet pump directly enters chlorination tail tank 10, the water of tail tank flows into afterbay 1, and the water of afterbay is recycled through handling again.Be delivered to tetrachloroethane tower 12 from the thick tetrachloroethane in the thick tetrachloroethane jar 11; after tetrachloroethane tower reboiler 13 heating rectifying separation; the rising gas phase is through tetrachloroethane tower complete condenser 14 and recirculated water heat exchange in the tower; phlegma flows into tetrachloroethane return tank 16; uncooled gas phase enters tetrachloroethane tail cooler 15 and chilled brine heat exchange; liquid phase flows into tetrachloroethane return tank 16; noncondensable gas emptying under nitrogen protection; material in the tetrachloroethane return tank refluxes mostly, and a small amount of extraction is to the finished product jar.Deliver to tetrachloroethane vaporizer 18 from the tetrachloroethane in the smart tetrachloroethane jar 17; gas after the vaporization enters dehydrochlorination reaction device feed preheater 21 and carries out heat exchange with the gas that dehydrochlorination reaction device 20 comes out; then to thermal oil preheater 19; after temperature required, enter dehydrochlorination reaction device 20 through heat-conducting oil heating; after the reacted mixed gas of dehydrochlorination reaction device is through 21 coolings of dehydrochlorination reaction device feed preheater, enter desorption tower 22; condensable gas is behind desorption tower complete condenser 24 usefulness circulating water coolings in the interior rising gas phase of tower; liquid phase enters desorption tower return tank 26; do not coagulate gas phase and enter desorption tower tail cooler 25; liquid phase flows into desorb return tank 26 after the condensation of the chilled brine degree of depth; noncondensable gas can be delivered to hydrogen chloride absorption workshop section; material in the desorption tower return tank all is back to desorption tower 22; the desorption tower reboiler 23 that connects on the desorption tower; heat to material; make a large amount of rising material steams is arranged in the tower; thereby make desorption tower still liquid acidity qualified; desorption tower still material enters desorption tower still flow container 27; material in the stripping vessel flow container is delivered to the low tower 28 that boils; through low tower reboiler 29 heating of boiling; after the rectifying separation; the rising gas phase is after low tower complete condenser 30 condensations of boiling in the tower; liquid phase enters the low tower return tank 32 that boils; uncondensed gas enters to hang down boils tower tail cooler 31 after the chilled brine heat exchange; liquid phase flows into the low tower return tank 32 that boils, noncondensable gas emptying under nitrogen protection.Material in the low tower return tank that boils refluxes mostly, and a small amount of extraction is to the finished product jar.Hang down and boil tower still mass transport to trieline tower 33; through 34 heating of trieline tower reboiler; after the rectifying separation; the rising gas phase is after the 35 recirculated water condensations of trieline tower complete condenser in the tower; phlegma enters trieline tower return tank 37; do not coagulate gas and enter trieline tower tail cooler 36 after the chilled brine condensation; liquid phase enters trieline tower return tank 37; do not coagulate gas emptying under nitrogen protection; trieline tower return tank inner condensat liquid is back to cat head; to the finished product jar, tower bottoms is delivered to trieline tower bottoms jar 39 to the cat head material through the side line extraction.Mass transport in the trieline tower bottoms jar 39 is to middle runnings tower 40; after material enters the middle runnings tower; through 41 heating of middle runnings tower reboiler; after the rectifying separation; rising steam is after middle runnings tower complete condenser 42 and recirculated water heat exchange in the tower; phlegma enters middle runnings tower return tank 44; after gas phase enters middle runnings tower tail cooler 43 and chilled brine heat exchange with fixed attention; liquid phase flows into middle runnings tower return tank 44; non-condensable gas emptying under nitrogen protection; the part of middle runnings tower return tank inner condensat liquid is back to the middle runnings column overhead through pipeline, and another part extraction is to desorption tower still flow container 27.The middle runnings tower bottoms is delivered to zellon tower 45; material in the zellon tower 45 heats through zellon tower reboiler; after the rectifying separation; rising steam is after zellon tower complete condenser 47 and recirculated water heat exchange in the tower; phlegma enters zellon tower return tank 49; after gas phase enters zellon tower tail cooler 48 and recirculated water heat exchange with fixed attention; liquid phase flows into zellon tower return tank 49; non-condensable gas emptying under nitrogen protection; the part of zellon tower return tank inner condensat liquid is back to the zellon column overhead through pipeline; another part extraction is to the zellon test tank, and tower bottoms is delivered to residual liquid tank.
Each entrance end links to each other by pipeline respectively with exit end.
Equipment such as pressure pump, hydraulic jet pump, chlorination tower, each rectifying tower, vaporizer, dehydrochlorination reaction device, each interchanger identical with existing corresponding device with principle of work.
Tetrachloroethane return tank 16 exit end link to each other with the import of finished product jar.
Triolefin discharging water cooler 38 exit end link to each other with the trieline test tank.
Zellon tower 45 lower part outlet ends also link to each other with the residual liquid tank entrance end.
Zellon tower return tank 49 exit end link to each other with zellon tower 45 entrance ends and zellon test tank entrance end through pipeline respectively.
As shown in Figure 3, described acetylene admission line links to each other with chlorination tower 9 entrance ends through acetylene gas dry decontamination device 50, on acetylene gas dry decontamination device 50, there is acetylene admission line 523 to link to each other with acetylene compressor 51 entrance ends, acetylene compressor 51 exit end link to each other with acetylene water cooler 52 entrance ends, acetylene cooler outlet end links to each other with acetylene spray catcher 53 entrance ends, acetylene spray catcher top exit end links to each other with the dry I tower of sulfuric acid 56 lower inlet ends, the dry I tower of sulfuric acid top exit end links to each other with the dry II tower of sulfuric acid 59 lower inlet ends, the dry II tower of sulfuric acid top exit end links to each other with the dry III tower of sulfuric acid 512 lower inlet ends, the dry III tower of sulfuric acid top exit end links to each other with acetylene acid separator 515 entrance ends, acetylene acid separator top exit end links to each other with acetylene adsorption tower 517 entrance ends, acetylene water cooler 52 another exit end link to each other with moisture holding tank 54 entrance ends, acetylene spray catcher 53 lower part outlet ends link to each other with moisture holding tank 54 entrance ends, vitriol oil storage tank 520 exit end link to each other with vitriol oil transferpump 522 entrance ends, vitriol oil transferpump exit end links to each other with concentrated sulfuric acid cooler 514 entrance ends, the concentrated sulfuric acid cooler exit end links to each other with the dry III tower of sulfuric acid 512 upper inlet ends, the dry III tower of sulfuric acid 512 lower part outlet ends link to each other with the dry II tower of sulfuric acid 59 lower inlet ends, the dry III tower of sulfuric acid 512 another lower part outlet ends link to each other with the dry III tower of sulfuric acid sulfuric acid recycle pump 513 entrance ends, the dry III tower of sulfuric acid sulfuric acid recycle pump 513 exit end link to each other with dilute sulphuric acid recirculation cooler 511 entrance ends, dilute sulphuric acid recirculation cooler 511 exit end link to each other with the dry III tower of sulfuric acid 512 upper inlet ends, the dry II tower of sulfuric acid 59 lower part outlet ends link to each other with the dry I tower of sulfuric acid 56 lower inlet ends, the dry II tower of sulfuric acid 59 another lower part outlet ends link to each other with the dry II tower of sulfuric acid sulfuric acid recycle pump 510 entrance ends, the dry II tower of sulfuric acid sulfuric acid recycle pump 510 exit end link to each other with another dilute sulphuric acid recirculation cooler 58 entrance ends, another dilute sulphuric acid recirculation cooler 58 exit end link to each other with the dry II tower of sulfuric acid 59 upper inlet ends, the dry I tower of sulfuric acid 56 lower part outlet ends link to each other with the dry I tower of sulfuric acid sulfuric acid recycle pump 57 entrance ends, the dry I tower of sulfuric acid sulfuric acid recycle pump 57 exit end link to each other with the 3rd dilute sulphuric acid recirculation cooler 55 entrance ends, the 3rd dilute sulphuric acid recirculation cooler 55 exit end link to each other with the dry I tower of sulfuric acid 56 upper inlet ends, the dry I tower of sulfuric acid 56 another lower part outlet ends link to each other with dilute sulphuric acid storage tank 519, and nitrogen buffer tank 521 links to each other with acetylene adsorption tower 517 lower inlet ends through nitrogen electric heater 518.
The concrete working process of dry decontamination device is, acetylene gas enters acetylene compressor 51, and to be compressed to that gaseous tension raises be 0.135 ~ 0.15Mpa, enter acetylene water cooler 52 again and be cooled to 2 ~ 5 ℃, cooled acetylene gas is after acetylene spray catcher 53 captures water smoke, enter the sulfuric acid drying of the dry I tower of sulfuric acid 56 usefulness about 88%, enter the sulfuric acid drying of the dry II tower of sulfuric acid 59 usefulness about 92% again, the vitriol oil that enters the dry III tower of sulfuric acid 512 usefulness 98% then is further dry, last acetylene gas is after acetylene acid separator 515 captures acid mist, entering the acetylene adsorption tower further purifies, acetylene gas after the processing is moisture at 60-70ppm, because the strong oxidizing property of the vitriol oil, also removed other impurity in the acetylene gas in the lump, acetylene gas has been played dewatering, the dual function that purifies.And traditional acetylene gas dry decontamination method adopts cold method, promptly with cool brine acetylene is cooled to about 0 ℃.Acetylene gas is moisture only can reduce to 200-300ppm, and temperature crosses the low pipeline that can make and freeze, and threatens ordinary production.
During first the driving, the water in acetylene spray catcher 53 and the moisture holding tank 54 is added by tap water pipeline.In normal productive process, the water of condensation that is got off by acetylene water cooler 52 and 53 condensations of acetylene spray catcher flows automatically respectively to moisture holding tank 54, regularly is disposed to trench then.
The concrete working process of sulfuric acid exsiccant is: be 98% the vitriol oil from the purity of vitriol oil storage tank 520, after being delivered to concentrated sulfuric acid cooler 514 cooling by vitriol oil transferpump 522, deliver to the dry III tower 512 of sulfuric acid, the dry II tower 59 of sulfuric acid was gone in overflow when the sulfuric acid in the dry III tower 512 of sulfuric acid surpassed certain liquid level, the sulfuric acid of the dry III tower of sulfuric acid 512 bottoms enters the dry III tower 512 of sulfuric acid after being delivered to 511 coolings of dilute sulphuric acid recirculation cooler by the dry III tower of sulfuric acid sulfuric acid recycle pump 513, forms the acid circulation.In the sulfuric acid drying
The dry I tower 56 of sulfuric acid, sulfuric acid drying were gone in overflow when the sulfuric acid in the tower 59 surpassed certain liquid level
The sulfuric acid of tower 59 bottoms enters the sulfuric acid drying after being delivered to another dilute sulphuric acid recirculation cooler 58 coolings by the dry II tower of sulfuric acid sulfuric acid recycle pump 510
Tower 59 forms the acid circulation.The sulfuric acid of the dry I tower of sulfuric acid 56 bottoms enters the dry I tower 56 of sulfuric acid after being delivered to 55 coolings of the 3rd dilute sulphuric acid recirculation cooler by the dry I tower of sulfuric acid sulfuric acid recycle pump 57, forms the acid circulation.The sulfuric acid liquid level of the dry I tower of sulfuric acid 56 bottoms drains into dilute sulphuric acid storage tank 519 when reaching certain level value.The acid mist that acetylene acid separator 515 captures flow to sulfuric acid holding tank 516 certainly, and then is disposed to dilute sulphuric acid storage tank 519.During first the driving, the sulfuric acid in each sulfuric acid tower and the acetylene acid separator 515 all will be injected into the regulation liquid level earlier by vitriol oil transferpump 522.
Nitrogen enters nitrogen buffer tank 521 through the nitrogen admission line, after 518 heating of nitrogen electric heater, enters acetylene adsorption tower 517.Each entrance end links to each other by pipeline respectively with exit end.The structure of equipment such as acetylene compressor, acetylene water cooler, acetylene spray catcher, each sulfuric acid tower, acetylene acid separator, acetylene adsorption tower, sulfuric acid cooler, nitrogen electric heater 518 is identical with existing corresponding device with principle of work.For improving cooling performance, can adopt two-stage acetylene water cooler, the exit end of elementary acetylene water cooler links to each other with secondary acetylene cooler inlet end, and the exit end of secondary acetylene water cooler links to each other with acetylene spray catcher 53 entrance ends.The acetylene adsorption tower adopts adsorbing tower with molecular sieve.
As shown in Figure 4, on described dehydrochlorination reaction device 20, at least 3 tetrachloroethane vaporizers 202 are arranged, also have the quantity dehydrochlorination reaction device 206 identical with the tetrachloroethane vaporizer, the import of each tetrachloroethane vaporizer links to each other with feeding line 201 through valve respectively, the outlet of each tetrachloroethane vaporizer links to each other through the import of valve with the dehydrochlorination reaction device respectively, the outlet of each dehydrochlorination reaction device links to each other with discharging pipeline 209 through valve respectively, between the outlet of each dehydrochlorination reaction device also through valve, pipeline 208 links to each other, between the import of each dehydrochlorination reaction device also through valve, another pipeline 205 links to each other, pipeline, link to each other by connection line 207 between another pipeline, the outlet of each tetrachloroethane vaporizer is also through valve, the 3rd pipeline 203 links to each other.
On this dehydrochlorination reaction device, every tetrachloroethane vaporizer and a dehydrochlorination reaction device are composed in series a group reaction system, simultaneously, by the connection control of pipeline and valve, the inlet line of every dehydrochlorination reaction device is that tetrachloroethane vaporizer outlet line and outlet line interconnect respectively.Like this, every tetrachloroethane vaporizer can with the series operation of arbitrary dehydrochlorination reaction device, and any two dehydrochlorination reaction devices can carry out series operation.Move two group reaction systems during ordinary production, a group reaction system reserve is promptly opened two and is equipped with one.When a certain group reaction system dehydrochlorination reaction catalyst activity reduction to 50% is following, stop this group reaction system operation, open the 3rd group reaction system.For further utilizing the activity of such catalysts in the dehydrochlorination reaction system of stopping, reduce the trieline unit consumption, with the outlet of the dehydrochlorination reaction device in the 3rd group reaction system connect with the dehydrochlorination reaction device import of stopping (the dehydrochlorination reaction device of promptly opening catalyst activity reduction again) move.Like this, can make full use of the dehydrochlorination activity of such catalysts, both can guarantee the high yield of dehydrochlorination reaction, avoid the waste of catalyzer again.The outlet of each tetrachloroethane vaporizer also links to each other through valve, the 4th pipeline 204 respectively.Dehydrochlorination reaction device by said structure, and the expansion of tetrachloroethane tower, desorption tower, low boil tower, trieline tower, middle distillate tower and zellon tower throughput, can make the present invention's trieline industrial production device reach the throughput of 4.0 ten thousand tons of/year trielines.
As Fig. 5-shown in Figure 8, on the gas distributor in described chlorination tower 9, main distribution pipe 91 is arranged, main distribution pipe two ends are horizontally connected with a short distribution pipe 92, the middle part is horizontally connected with the distribution pipe 94 of drawing money on credit, short distribution pipe, draw money on credit have between the distribution pipe in distribution pipe 93 cross connection on main distribution pipe, have one to discharge pore 101 respectively in vertical direction, the vertical direction both sides of main second circumference of distribution pipe tube wall, on second circumference of each distribution pipe tube wall, be distributed with many row's distribution pipe production wells 301.
During use, pack into gas distributor in the chlorination tower after, at the two ends of each distribution pipe closure plate 95 is installed, and is fixed on by U-bolt 910 on the fabricated section of acetylene chlorination inner wall of tower.At the end of main distribution pipe another closure plate 96 is installed, and is fixed on the fabricated section of acetylene chlorination inner wall of tower by another U-bolt 911.Each distribution pipe can pass main distribution pipe, has through hole 302 to communicate with main distribution pipe inner chamber on the distribution pipe.The nut 98 that passes main, as to prop up distribution pipe bolt 97 and bolt two ends will be led, a distribution pipe is fixed together.Gas enters from the port 99 that main distribution pipe is exposed at acetylene chlorination tower outside, and the production well on each pipe is distributed in the acetylene chlorination tower.The gas distributor of this structure has improved chlorine, its distribution effect in chlorination mother solution of acetylene, obviously strengthened the distribution effect of gas, improved the yield of chlorination reaction, the purity of thick tetrachloroethane remains on 97-98%, exceeds 3-4% than the domestic same industry.Prevented because of skewness, reacted not exclusively that acetylene gas contacts the phenomenon of blasting with chlorine.
Trieline tower complete condenser shell side, trieline discharging water cooler shell side, trieline test tank, trieline storage tank material are replaced by stainless steel by carbon steel, guaranteed that effectively the trieline product has colourity preferably, avoided the pollution of the corrosion of carbon steel material product.
The rectifying section of tetrachloroethane tower, the rectifying section of desorption tower adopt the enamel material, and the low tower rectifying section that boils adopts fluorinated ethylene propylene (F40) tower joint.For improving the rectification effect of trieline tower, this tower is designed to valve tray column.For improving tower tray work-ing life, float valve and tower tray material are designed to stainless steel.The resistance to corrosion and the rectification effect of each tower rectifying section have been improved like this, greatly.
Trieline and other intermediates are under the situation that has oxygen to exist, and the generation organic acid that can react causes the rotten of product and consumes and rises.For avoiding trieline and other intermediates to contact with oxygen, nitrogen seal device is used in design on the test tank of intermediate tank farm and finished product tank field, storage tank, and the redundant space in the container is occupied by nitrogen.Guarantee the quality of product, avoided the decomposition of trieline.
The raw material of producing trieline is chlorine and acetylene, and chlorine is hypertoxic medium, and acetylene chemistry character is active, and is inflammable and explosive.For further improving the security of producing, the present invention's device has been set a plurality of interlockings, be respectively the interlocking of acetylene compressor import and export pressure and compressor, the interlocking of compressor and chlorine, acetylene variable valve, the interlocking of tail water flow and chlorine, acetylene gas variable valve, the interlockings of chlorination tower vacuum tightness and chlorine, acetylene variable valve etc. have been guaranteed safety, the steady running of trieline device by above interlocking.
The chlorination tower moves under negative pressure state, and negative pressure is aspirated generation with hydraulic jet pump.In the process of suction, part hydrogen chloride gas, acetylene gas, chlorine and organic acid are dissolved in the tail water, cause tail water acidity to be strengthened gradually.Other trieline producers when tail water acidity reaches certain numerical value, just replace tail water, have not only polluted environment but also wasted water resources.The present invention's device is delivered to hydraulic jet pump with the tail water in the afterbay with the tail water force (forcing) pump, the chlorination tower is aspirated make it to produce negative pressure, and tail water, recycles to afterbay by the overflow of chlorination tail tank, has saved great amount of water resources, has protected environment.
The trieline tower of other trieline producers adopts the discharging of trim the top of column liquid, product contains acid at 10-15ppm or higher, when being used as trieline and being metal cleaner and using, can erode metallic surfaces, the object that destruction is cleaned is to causing serious loss with trieline as the producer of clean-out system.On the present invention's the device, the trieline tower is set up four side discharge ports, is located at respectively on the 5th, 7,9, the 11 layer of tower tray of rectifying section.The cat head discharging combines with the upper side discharge method, can effectively reduce trieline product acidity, and acidity can be controlled in below the 5ppm.
Claims (4)
1. trieline industrial production device, it is characterized in that, it has the acetylene admission line to link to each other with chlorination tower (9) entrance end respectively with the chlorine admission line, chlorination tower (9) exit end links to each other with chlorination tower complete condenser (7) entrance end, chlorination tower complete condenser (7) exit end links to each other with chlorination return tank (8) entrance end and chlorination tower tail cooler (6) entrance end respectively, chlorination tower tail cooler (6) exit end links to each other with chlorination return tank (8) entrance end and gas-liquid separator (5) entrance end respectively, gas-liquid separator (5) exit end links to each other with tail gas buffer (4) entrance end, tail gas buffer (4) exit end links to each other with hydraulic jet pump (3) entrance end, hydraulic jet pump (3) exit end links to each other with chlorination tail tank (10) entrance end, chlorination tail tank (10) exit end links to each other with chlorination afterbay (1) entrance end, chlorination afterbay (1) exit end links to each other with pressure pump (2) entrance end, pressure pump (2) exit end links to each other with another entrance end of hydraulic jet pump (3), chlorination return tank (8) exit end links to each other with thick tetrachloroethane jar (11) entrance end, thick tetrachloroethane jar (11) exit end links to each other with tetrachloroethane tower (12) entrance end, tetrachloroethane tower (12) lower part outlet end links to each other with tetrachloroethane tower reboiler (13) entrance end and smart tetrachloroethane jar (17) entrance end respectively, tetrachloroethane tower reboiler (13) exit end links to each other with another entrance end of tetrachloroethane tower (12), tetrachloroethane tower (12) top exit end links to each other with tetrachloroethane tower complete condenser (14) entrance end, tetrachloroethane tower complete condenser (14) exit end links to each other with tetrachloroethane tower return tank (16) entrance end and tetrachloroethane tower tail cooler (15) entrance end respectively, tetrachloroethane tail cooler (15) exit end links to each other with tetrachloroethane tower return tank (16) entrance end, smart tetrachloroethane jar (17) exit end links to each other with tetrachloroethane vaporizer (18) entrance end, tetrachloroethane vaporizer exit end links to each other with dehydrochlorination reaction device feed preheater (21) entrance end, dehydrochlorination reaction device feed preheater (21) exit end links to each other with thermal oil preheater (19) entrance end, thermal oil preheater (19) exit end links to each other with dehydrochlorination reaction device (20) entrance end, dehydrochlorination reaction device (20) exit end links to each other with another entrance end of dehydrochlorination reaction device feed preheater (21), another exit end of dehydrochlorination reaction device feed preheater (21) links to each other with desorption tower (22) entrance end, desorption tower (22) outlet at bottom end links to each other with desorption tower reboiler (23) entrance end, desorption tower reboiler (23) exit end links to each other with another entrance end of desorption tower (22), desorption tower top exit end links to each other with desorption tower complete condenser (24) entrance end, desorption tower complete condenser exit end links to each other with desorption tower return tank (26) entrance end and Analytic Tower tail cooler (25) entrance end respectively, Analytic Tower tail cooler (25) exit end links to each other with desorption tower return tank (26) entrance end, desorb return tank (26) exit end links to each other with extraction-container flow container (27) entrance end, extraction-container flow container (27) exit end links to each other with low tower (28) entrance end that boils, low tower (28) the lower part outlet end that boils links to each other with low tower reboiler (29) entrance end and trieline tower (33) entrance end of boiling respectively, the low tower reboiler exit end that boils links to each other with low another entrance end of tower that boils, low tower (28) the top exit end that boils links to each other with low tower complete condenser (30) entrance end that boils, low tower complete condenser (30) exit end that boils reaches low tower tail cooler (31) entrance end that boils with low tower return tank (32) entrance end that boils respectively and links to each other, low tower tail cooler (31) exit end that boils links to each other with low tower return tank (32) entrance end that boils, trieline tower (33) lower part outlet end links to each other with trieline tower reboiler (34) entrance end and trieline still flow container (39) entrance end respectively, trieline tower reboiler (34) exit end links to each other with another entrance end of trieline tower (33), trieline tower (33) top exit end links to each other with trieline tower complete condenser (35) entrance end, trieline tower complete condenser (35) exit end links to each other with trieline tower tail cooler (36) entrance end and trieline tower return tank (37) entrance end respectively, trieline tower tail cooler (36) exit end links to each other with trieline return tank (37) entrance end, trieline return tank (37) exit end respectively with another entrance end of trieline tower (33), trieline discharging water cooler (38) entrance end links to each other, trieline still flow container (39) exit end links to each other with middle runnings tower (40) entrance end, middle runnings tower (40) lower part outlet end links to each other with middle runnings tower reboiler (41) entrance end and zellon tower (45) entrance end respectively, middle runnings tower (40) top exit end links to each other with middle runnings tower complete condenser (42) entrance end, middle runnings tower complete condenser (42) exit end links to each other with middle runnings tower tail cooler (43) entrance end and middle runnings tower return tank (44) entrance end respectively, middle runnings tower tail cooler (43) exit end links to each other with another entrance end of middle runnings tower return tank (44), middle runnings tower return tank (44) exit end links to each other with another entrance end of desorption tower still flow container (27), zellon tower (45) lower part outlet end and zellon tower reboiler (46) entrance end, zellon tower (45) top exit end links to each other with zellon tower complete condenser (47) entrance end, zellon tower complete condenser (47) exit end links to each other with zellon tower return tank (49) entrance end and zellon tail cooler (48) entrance end respectively, zellon tail cooler (48) exit end links to each other described each complete condenser with another entrance end of zellon tower return tank (49), the heat exchange device of each tail cooler adopts the graphite piece of modified phenolic resin impregnate with tallow.
2. trieline industrial production device as claimed in claim 1, it is characterized in that, described acetylene admission line links to each other with chlorination tower (9) entrance end through acetylene gas dry decontamination device (50), on acetylene gas dry decontamination device (50), there is acetylene admission line (523) to link to each other with acetylene compressor (51) entrance end, acetylene compressor (51) exit end links to each other with acetylene water cooler (52) entrance end, acetylene cooler outlet end links to each other with acetylene spray catcher (53) entrance end, acetylene spray catcher top exit end links to each other with dry I tower (56) the lower inlet end of sulfuric acid, the dry I tower of sulfuric acid top exit end links to each other with dry II tower (59) the lower inlet end of sulfuric acid, the dry II tower of sulfuric acid top exit end links to each other with dry III tower (512) the lower inlet end of sulfuric acid, the dry III tower of sulfuric acid top exit end links to each other with acetylene acid separator (515) entrance end, acetylene acid separator top exit end links to each other with acetylene adsorption tower (517) entrance end, another exit end of acetylene water cooler (52) links to each other with moisture holding tank (54) entrance end, acetylene spray catcher (53) lower part outlet end links to each other with moisture holding tank (54) entrance end, vitriol oil storage tank (520) exit end links to each other with vitriol oil transferpump (522) entrance end, vitriol oil transferpump exit end links to each other with concentrated sulfuric acid cooler (514) entrance end, the concentrated sulfuric acid cooler exit end links to each other with dry III tower (512) the upper inlet end of sulfuric acid, dry III tower (512) the lower part outlet end of sulfuric acid links to each other with dry II tower (59) the lower inlet end of sulfuric acid, dry another lower part outlet end of III tower (512) of sulfuric acid links to each other with dry III tower sulfuric acid recycle pump (513) entrance end of sulfuric acid, dry III tower sulfuric acid recycle pump (513) exit end of sulfuric acid links to each other with dilute sulphuric acid recirculation cooler (511) entrance end, dilute sulphuric acid recirculation cooler (511) exit end links to each other with dry III tower (512) the upper inlet end of sulfuric acid, dry II tower (59) the lower part outlet end of sulfuric acid links to each other with dry I tower (56) the lower inlet end of sulfuric acid, dry another lower part outlet end of II tower (59) of sulfuric acid links to each other with dry II tower sulfuric acid recycle pump (510) entrance end of sulfuric acid, dry II tower sulfuric acid recycle pump (510) exit end of sulfuric acid links to each other with another dilute sulphuric acid recirculation cooler (58) entrance end, another dilute sulphuric acid recirculation cooler (58) exit end links to each other with dry II tower (59) the upper inlet end of sulfuric acid, dry I tower (56) the lower part outlet end of sulfuric acid links to each other with dry I tower sulfuric acid recycle pump (57) entrance end of sulfuric acid, dry I tower sulfuric acid recycle pump (57) exit end of sulfuric acid links to each other with the 3rd dilute sulphuric acid recirculation cooler (55) entrance end, the 3rd dilute sulphuric acid recirculation cooler (55) exit end links to each other with dry I tower (56) the upper inlet end of sulfuric acid, dry another lower part outlet end of I tower (56) of sulfuric acid links to each other with dilute sulphuric acid storage tank (519), and nitrogen buffer tank (521) links to each other with acetylene adsorption tower (517) lower inlet end through nitrogen electric heater (518).
3. trieline industrial production device as claimed in claim 1 or 2, it is characterized in that, on described dehydrochlorination reaction device (20), at least 3 tetrachloroethane vaporizers (202) are arranged, also have the quantity dehydrochlorination reaction device (206) identical with the tetrachloroethane vaporizer, the import of each tetrachloroethane vaporizer links to each other with feeding line (201) through valve respectively, the outlet of each tetrachloroethane vaporizer links to each other through the import of valve with the dehydrochlorination reaction device respectively, the outlet of each dehydrochlorination reaction device links to each other with discharging pipeline (209) through valve respectively, between the outlet of each dehydrochlorination reaction device also through valve, pipeline (208) links to each other, between the import of each dehydrochlorination reaction device also through valve, another pipeline (205) links to each other, pipeline, link to each other by connection line (207) between another pipeline, the outlet of each tetrachloroethane vaporizer is also through valve, the 3rd pipeline (203) links to each other.
4. as claim 1 or 2 or 3 described trieline industrial production devices, it is characterized in that, on the gas distributor in described chlorination tower (9), main distribution pipe (91) is arranged, main distribution pipe two ends are horizontally connected with a short distribution pipe (92), the middle part is horizontally connected with the distribution pipe of drawing money on credit (94), a short distribution pipe, draw money on credit have between the distribution pipe in distribution pipe (93) cross connection on main distribution pipe, vertical direction at main second circumference of distribution pipe tube wall, the vertical direction both sides have one to discharge pore (101) respectively, are distributed with many row's distribution pipe production wells (301) on second circumference of each distribution pipe tube wall.
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| CN 201010188455 CN102267868B (en) | 2010-06-01 | 2010-06-01 | Industrial production apparatus for trichloroethylene |
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| CN102775269A (en) * | 2012-07-13 | 2012-11-14 | 中国石油集团东北炼化工程有限公司葫芦岛设计院 | Trichloroethylene gas phase catalysis production method |
| CN103467240A (en) * | 2013-09-23 | 2013-12-25 | 芜湖融汇化工有限公司 | System for separating hydrogen chloride in coarse trichloroethylene |
| CN108438579A (en) * | 2018-03-23 | 2018-08-24 | 江苏安邦电化有限公司 | A kind of N-butyl raw material finished product storage tank nitrogen seal device |
| CN110479124A (en) * | 2019-08-09 | 2019-11-22 | 浙江衢州巨塑化工有限公司 | A kind of tetrachloroethanes process units and its method |
| CN111087280A (en) * | 2020-01-22 | 2020-05-01 | 辽宁方大工程设计有限公司 | Production method for preparing trichloroethylene by acetylene chlorination-gas phase catalytic dehydrochlorination |
| CN114272885A (en) * | 2021-12-28 | 2022-04-05 | 厦门中科易工化学科技有限公司 | Tower reactor for synthesizing chloroethylene and application thereof |
| CN114455221A (en) * | 2022-03-14 | 2022-05-10 | 滨化集团股份有限公司 | System and method for controlling tank top pressure of normal-pressure storage tank with nitrogen seal |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108438579A (en) * | 2018-03-23 | 2018-08-24 | 江苏安邦电化有限公司 | A kind of N-butyl raw material finished product storage tank nitrogen seal device |
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| CN111087280B (en) * | 2020-01-22 | 2023-08-29 | 辽宁方大工程设计有限公司 | Production method for preparing trichloroethylene by acetylene chlorination-gas phase catalytic dehydrochlorination |
| CN114272885A (en) * | 2021-12-28 | 2022-04-05 | 厦门中科易工化学科技有限公司 | Tower reactor for synthesizing chloroethylene and application thereof |
| CN114455221A (en) * | 2022-03-14 | 2022-05-10 | 滨化集团股份有限公司 | System and method for controlling tank top pressure of normal-pressure storage tank with nitrogen seal |
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Denomination of invention: Industrial production apparatus for trichloroethylene Effective date of registration: 20190102 Granted publication date: 20130619 Pledgee: Binzhou Bincheng Branch of China Construction Bank Co., Ltd. Pledgor: Befar Group Co.,Ltd. Registration number: 2018370000240 |
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