Method of producing vinylchloride

专利摘要:
The invention relates to the production of halohydrocarbons, in particular the production of vinyl chloride, used to synthesize polymers. The goal is to increase the degree of cleavage of 1,2-dichloroethane (DCE) and reduce energy consumption in the process. The latter is carried out in a pyrolysis oven, which serves pre-evaporated DCE. At the same time, liquid DCE is indirectly heated to boiling (197-270 ° C) with the help of hot vinyl chloride-containing gases with a temperature of 500-533 ° C (formed in the pyrolysis furnace) in an additional (1st) tank. Then boiling DCE is transferred to the 2nd tank, where, without heating at a pressure of 1.2-3.7 MPa, DCE is evaporated in an amount of 6-9 kg / h per 100 kg / h of DCE circulating in both tanks . In this case, non-evaporated DCE from the 2nd tank is returned to the 1st tank. Liquid fresh source DCE is preheated with flue gases in the convective zone of the pyrolysis furnace or in the heat exchanger up to 150–195 ° C and then introduced into the 2nd tank in the amount of 6.25– 9.3 kg / h per 100 kg / h circulating in both capacitances DCE. In addition, for every 100 kg / h of fresh fresh EDC injected from the 1st tank, 3–3.6 kg / h of liquid DCE is combined with the impurities formed during evaporation and sent to the stage of separation of pure DCE. It is better to thermostatically adjust the temperature of the level of liquid supplied to the 2nd tank depending on the height of the liquid level in the 2nd tank. These conditions make it possible to obtain 29.5% more vinyl chloride with a 22.1% lower distillation (repeated) of 1,2-dichloroethane, thereby achieving a reduction in energy consumption. The target product on the content of butadiene in it is cleaner than in the known case (2 times). The degree of cleavage of 1,2-dichloroethane is 65% versus 50%. 1 hp f-ly, 3 ill., 1 tab.
公开号:SU1598862A3
申请号:SU874203496
申请日:1987-10-09
公开日:1990-10-07
发明作者:Линк Герхард；Фрелих Вальтер；Крумбек Райнхард；Прантль Георг；Шаффельхофер Иво
申请人:Хехст Аг (Фирма)；Уде Гмбх (Фирма)；
IPC主号:

专利说明:

The invention relates to a method for producing vinyl chloride by splitting 1,2-dichloroegan, which finds use as a monomer for polymeric materials.
The aim of the invention is to increase the degree of cleavage of 1,2-dichloroethane and reduce energy costs.
FIG. 1 to 3 are flow charts for insuring the proposed method.
Example 1. Act according to the technological scheme shown in FIG. 1. From collection 1, 834 kg of 1,2-dichloroethane is withdrawn in 1 hour at
130 C and with the help of pump 2 under pressure 0
The second and second tanks of 1,2-dichloro ethane are 133344 kg / h. For every 100 kg / h circulating between the first tank 7 and the second tank of liquid 1,2-dichloroethane, 6.25 kg / h of fresh liquid 1,2-dichloroethane is introduced into the second tank 6. Evaporated mainly in upward leading pipes
At 4.0 MPa and at 125 ° C, the 1,2-dichloric region of the pyrolysis furnace convective zone 3 is fed to NIJ-JQ and in the second tank 6. The exhaust gases 4 and gases from the radioactive zone 4 of the pyrolysis furnace heat liquid 2.2-dichloroethane to 220 s, and the flue gases j are cooled from 930 to. In the heat exchanger 5, energy is absorbed between the energy-releasing liquid 1,2-dichloroethane region 3 and the power consumption in the first tank, 20 necessary for the extraction of 1,2-dichloroethane. To this end, using a conventional device (LIC), measure the level of liquid 1,2-dichloroethane | in the second tank 6 and, based on this 25 measured value, as a controlled quantity, is supplied in the required amount to the heat exchanger 5 under pressure 2 , 5 MPa boiler feedwater
ethane in the form free from liquid or solid components is introduced through a pipe 10 into the radiation zone 4 of a polarized furnace, in which the 1,2-dichloroethane gas is heated using four rows of burners 11 one above the other above 533 ° C . The lower and upper rows of burners are loaded with a similar amount of fuel.
During gas overheating up to 533
a part of 1,2-dichloroethane is decomposed into vinyl chloride and hydrogen chloride. Hot pyrolysis gases are sent to the first tank 7 through a pipeline and they leave this tank with temperature. The average cooling rate of perolysis gases in the first vessel 7 is 46 C / s, i.e. 1 / 11.6 inlet temperature (533 C) per second. Pipeline 13 provides these pyrolysis gases for further cooling in accordance with the prior art (not shown), and they are partially condensed. According to a known method, hydrogen sulfide is separated from the mixture of substances developed as a result of thermal cleavage, according to a known method, in a column (not shown) at a temperature of -24 ° C. The pressure at the top of the tank is set so that the gas-shaped evaporated 1,2-dichloroethane leaves the second tank 6 at a tempo rture of 270 C. In this tank, 804 kg / h of 1,2-dichloroethane are evaporated at
Ib as a cooling agent. Dp cooling requires 210 dm. Of boiler feedwater, which in this case heats up to 80 and leaves the heat exchanger 5 through the pipeline. The amount of regenerated energy is 185.7 kJ / kg vinyl chloride.
Cooled to approximately 185 ° C, 1,2-dichloroethane is fed through a loop of pipe with evenly distributed openings into the second tank 6 and mixed there with hotter 1,2-dichloroethane, which rises from the first tank 7 through pipes 8 to the second tank part of this 1,2-dichloroethane is evaporated. In the first vessel 7, liquid 1,2-dichloroethane is formed by heat exchange with a hot gas containing effluent from the radiation. zone 4 of the PHYLYSIC furnace by pipeline vinyl chloride, heated to boiling. The heat exchange is facilitated by the natural circulation of 1,2-dichloroethane between the first tank 7 and the second tank 6 through the lifting pipes 8 and the pipes leading downwards 9. The mixture of liquid and gas in the lifting pipes 8 has a temperature of 270 ° C, the liquid in the downward leading pipes 9 - the temperature is 263 C. The amount of 1,2-dichloroethane circulating between the first and second tanks is 133344 kg / h. For every 100 kg / h circulating between the first tank 7 and the second tank 6 liquid 1,2-dichloroethane, 6.25 kg / h of fresh liquid 1,2-dichloroethane is introduced into the second tank 6. Evaporated mainly in upward leading pipes 8
ethane in a form free from liquid or solid components is introduced through conduit 10 into the radiation zone 4 of the pyrolysis furnace, in which the gaseous 1,2-dichloroethane is heated using four rows of burners 11 arranged one above the other to 533 ° C. The lower and upper rows of burners are loaded with fuel in the same quantity.
During gas overheating to

a portion of 1,2-dichloroethane is split into vinyl chloride and hydrogen chloride. The hot pyrolysis gases are directed to the first tank 7 through conduit 12 and they exit from that tank with a temperature. The average cooling rate of perolysis gases in the first tank 7 is 46 C / s, i.e. . ; 1 / 11.6 inlet temperature (533 C) per second. Pipe 13 provides these pyrolysis gases for further cooling according to the prior art (not shown), and they are partially condensed. From a mixture of substances formed as a result of thermal cleavage, according to a known method, hydrogen chloride is separated in a column (not shown) at a temperature of -24 ° C. The pressure at the top of the column is set so that the gaseous evaporated 1,2-dichloroethane leaves the second tank 6 with a temperature of 270 C. In this tank 804 kg / h of 1,2-dichloroethane are evaporated at
pressure of 3.7 MPa, which corresponds to 6.0 kg / h for every 100 kg / h of liquid 1,2-dichloroethane circulating between the first 7 and second 6 containers. 2880 kg / h of 1,2-dichloroethane is evaporated to each square meter of the surface area of the liquid taken in the second tank 6 as stationary. From the bottom of the first tank 7, 30 kg / h of liquid 1,2-dichloroethane is discharged.
and through the pipeline 14 is fed into the column, in which the distillation of 1,2-dichloroethane through the top (not shown). THIS is 3.6 kg / h of 1,2-dichloroethane removed from the first tank of 7 for each
1598862
100 kg / h of fresh 1,2-di chloroethane entering the second tank 6. The average residence time of 1,2-dichloroethane in the first and second containers is 47 minutes in total.
The burners 11 in the pyrolysis furnace through the pipeline are supplied with fuel (methane) in a volume of O, 103 nm per 1 kg of vinyl chloride obtained. The hot flue JQ gases, whose temperature at the exit from the preheating zone of 1,2-dichloroethane is TU, are cooled before heating to steam and hot water before being released into the atmosphere. In the upper part 15 of the convective zone 3 of the pyroln-type furnace, the cold water supplied through the pipeline 15 is heated, which is partially supplied through the pipeline 16 to
Pyrolysis gas furnaces generate hot water and high steam, 185.7 + 178.3 + 843, 1208.4 kJ / kg of winch chloride, which corresponds to fuel consumption (methane) in the amount of 0.034 vinyl chloride. Thereby, the effective consumption of combustible gas is reduced to 0.069 nm of the ACG of vinyl chloride, which is co-. It consumes only 67.4% of the flow rate (100%) with comparative experience. Energy saving is 32.6% with an increase in the degree of cleavage within 55–65% and an increase in the service life of the pyrolysis furnace within 6–9 months.
PRI mme R 2. Act according to the technological scheme shown
boiler 17, and partly through the pipeline— ”FIG. 2. Types of equipment are the same
for use in other parts of the process. Hot water from boiler 17 is supplied through a pipeline to the middle part of the convective zone 3 of the pyrolysis furnace, and after the heat from the rising flue gases is absorbed by pipeline 18, it is again fed to the boiler 17. The steam generated there is drained through pipeline 19 and is used for
as in example 1. The method of example 2 is different from the method of example 1 by the following points.
25 From the collection, 834 kg of 1,2-dichloroethane are withdrawn in 1 hour with and with the help of a pump under pressure of 2.9 MGT and at 125 ° C through the heat exchanger 5 through the pipeline they are fed without heating s into other parts of the process of obtaining the viral target zone 3 Nilyl chloride furnaces. 114 kg / h of high pressure steam (2.1 MPa, 215 s) are obtained and discharged through line 18. The energy regenerated in this process is 843.9 kJ / kg of vinyl chloride. By pipe-, "line 20, 201 hot water is withdrawn with a temperature of energy regenerated in this case of 178.8 kJ / kg vinyl chloride.
The degree of cleavage of 1,2-dichloroethane in the radiation zone 4 of the pyrolysis furnace is 65%. 330 kg of vinyl chloride are obtained in 1 hour. After 9 months of operation of the heat exchange furnace and liquid 1,2-dichloroethane in the first tank 7 remains almost unchanged. The temperature difference between the hot gases from the pyrolysis furnace, which are removed through conduit 13 from the first tank 7, and the gaseous 1,2-dichloroethane, which leaves the second tank 6, and through conduit 10 is fed into the pyrolysis oven. em 10 ° C. On the heat exchange surfaces, neither on the side of hot pyrolysis gases, nor on the side of liquid 1,2-dichloroethane, there was no noticeable bloom. Energy recovered from flue
45
mediocre to the second tank 6. The heat exchanger 5 is heated by high-pressure steam (2.1 KiTIa 215 s) from the boiler 17 through the pipeline. By measuring the level of liquid 1,2-dichloroethne (LIC) from the second tank 6, the high-pressure steam is regulated as an adjustable parameter. pressure on the heat exchanger 5. The temperature of 1,2-dichloro ethane at the exit of the heat exchanger is. Hot vinyl chloride containing pyrolysis gases are released from the radiation zone 4 pyrols. In a furnace at 533 ° C, the furnace passes through the first vessel 7 and leaves it at. The cooling rate of hot pyrolysis gases in the first vessel 7 is 51.7 ° C / s, which is 1 / 10.3 of the temperature at the entrance () in this capacity in 1 s. After exiting the first vessel, the pyrolysis gases are, according to a known method, subjected to further cooling and hydrogen chloride is distilled off in a column with a top temperature of -31 s. The pressure at the top of this column is set in such a way that 1,2-dichloroethane leaves the second tank 6 under pressure 1598862
the pyrolysis furnace gasses generate hot water and high steam, 185.7 + 178.3 + 843.9 1208.4 kJ / kg of winch chloride, which corresponds to fuel consumption (methane) in an amount of 0.034 vinyl chloride. This reduces the effective flow rate of the combustible gas to 0.069 nm ACC of vinyl chloride, which reduces the co-absorption to only 67.4% of the flow rate (100%) with comparative experience. At the same time, energy saving is 32.6% with an increase in the degree of cleavage within 55–65% and an increase in the service life of the pyrolysis furnace within 6–9 months.
PRI mme R 2. Act according to the technological scheme shown
„And FIG. 2. Types of equipment are the same
as in example 1. The method of example 2 is different from the method of example 1 by the following points.
834 kg of 1,2-dichloroethane is withdrawn from the collection in 1 hour with and with the help of a pump under pressure of 2.9 MGTa and at 125 ° C through the heat exchanger 5 through the pipeline it is fed without charging the convection zone 3 of the furnace.
five
mediocre to the second tank 6. The heat exchanger 5 is heated by high-pressure steam (2.1 KiTIa 215 s) from the boiler 17 through the pipeline. By measuring the level of liquid 1,2-dichloroethne (LIC) from the second tank 6, the high-pressure steam is regulated as an adjustable parameter. pressure on the heat exchanger 5. The temperature of 1,2-dichloro ethane at the exit of the heat exchanger is. Hot vinyl chloride-containing pyrolysis gases are released from the radiation zone 4 pyrols. In a furnace at 533 ° C, the furnace passes through the first vessel 7 and leaves it at. The cooling rate of hot pyrolysis gases in the first vessel 7 is 51.7 ° C / s, which is 1 / 10.3 of the temperature at the entrance () in this capacity in 1 s. After exiting the first vessel, the pyrolysis gases are, according to a known method, subjected to further cooling and hydrogen chloride is distilled off in a column with a top temperature of -31 s. The pressure at the top of this column is set in such a way that 1,2-dichloroethane leaves the second tank 6 under a pressure of 2.6 Mlla and with a temperature of 240 s. In this tank and in the riser pipes, 804 kg of 1,2-dichloroethane are evaporated in 1 hour, which is then fed via conduit 10 to the radiation zone of the pyrolysis furnace. For every 100 kg / h circulating between the first 7 and second 6 tanks of liquid 1,2-dichloroethane, 6.1 kg / h are evaporated.
The temperature in the riser pipes is 240 ° C, and in the down pipes it is 235 C.
between 7 and 7, and the second with 6 tanks of liquid 1,2-dichloroethane is 13177 kg / h. For every 100 kg / h circulating - between the first and second tanks of 1,2-dichloroethane. At the bottom of the first tank 7, 30 kg / h of liquid 1,2-dichloroethane is withdrawn through the pipeline and fed into the column in which 1,2-dichloroethane is distilled through the top and fed into the column in which 1,2- dichloro-25 ethane, i.e. 3.6 kg / h for every 100 kg / h received in the second tank of 1,2-dichloroethane. The average residence time of 1,2-dichloroethane in the first and second tanks as a whole is 47 minutes, for every square meter of the liquid taken as the stationary surface of the second tank 6 2880 kg -1,2-dichloroethane is evaporated in 1 hour.
Four pyrolysis furnaces located one above the other in a row of burners 11 supply the pipeline with fuel (methane) in a total volume of 0.1074 nm per 1 kg of vinyl chloride produced. In the upper part of the convective zone 3 of the pyrolysis furnace, 330 boiler feedwater (pressure 2.5 MPa) is heated in the economizer and supplied through the pipeline at 80 ° C, and partially through the pipeline is fed to the boiler 17, then partially through the pipeline in another part of the vinyl chloride process. As in example 1, the liquid from the boiler 17 is heated in the lower part of the convective zone 3 and is fed to the boiler 17 through the pipeline. A part of the steam o produced in the boiler 17 is used to heat the heat exchanger 5. Most of this steam, namely 167 kg / h, is used in other parts of the process to produce vinyl chloride. As a result, 1236.2 kJ of energy per 1 kg of vinyl chloride is regenerated. By pipeline directed 1598862I
136 dm / h of feed water of the boiler at 150 ° C for reuse, resulting in regenerated energy in the volume of 121 kJ per 1 kg of vinyl chloride. The total regenerated energy facility is 1236.2 + 121 1357.2 kJ / kg vinyl chloride, which corresponds to fuel consumption (methane). IQ of 0.038 HMVKr of vinyl chloride. The effective consumption of combustible gas is thereby reduced to 0.694, which is only 67.8% of the consumption (100%), which was required in comparative experience. Energy savings are respectively 32.2%. As in Example 1, after 9 months of operation, no matter how much noticeable raids on the heat exchange surfaces in
35
40
50
55
the first tank 7 is not marked; the service life of the pyrolysis furnace is also at least 9. months. 330 kg of vinyl chloride are obtained in 1 hour, the degree of cleavage of 1,2-dichloroethane is 65%.
PRI mme r.3. Act according to the technological scheme shown in FIG. 3. From collection 1, 780 kg of 1,2-dichloroethane is withdrawn in 1 hour at 130 ° C and with the help of a pump under a pressure of 3.6 MPa and fed into the middle part of the convective zone. 3 pyrolysis ovens. Through the diverted flue gases from the radioactive zone of the pyrolysis furnace, liquid 1,2-dichloroethane is heated to 210 s. In the heat exchanger 5, energy is converted between the zone that gives energy to liquid 1,2-dichloroethane and energy consumption for evaporation of 1,2-dichloroethane in. the first tank 7. To this end, the level of liquid 1,2-dichloroethane in the second tank 6 and starting from is measured using a known device (LIC). of this measured value as a controlled parameter, the required amount of boiler feedwater under a pressure of 2.5 MPa as a cooling agent is fed into the heat exchanger 5 through a pipeline. For cooling, 180 dm of boiler feedwater is required, which in this case heats up to 100 and leaves the heat exchanger 5 through the pipeline. The amount of regenerated energy is 73.5 kJ / kg vinyl chloride.
Cooled. Up to 195 with 1,2-dichloroethane is fed through a loop of a pipeline with evenly distributed openings.

the first tank 7 is not marked; the service life of the pyrolysis furnace is also at least 9. months. 330 kg of vinyl chloride are obtained in 1 hour, the degree of cleavage of 1,2-dichloroethane is 65%.
PRI mme r.3. Act according to the technological scheme shown in FIG. 3. From collection 1, 780 kg of 1,2-dichloroethane is withdrawn in 1 hour at 130 ° C and with the help of a pump under a pressure of 3.6 MPa and fed into the middle part of the convective zone. 3 pyrolysis ovens. Through the diverted flue gases from the radioactive zone of the pyrolysis furnace, liquid 1,2-dichloroethane is heated to 210 s. In the heat exchanger 5, energy is converted between the zone that gives energy to liquid 1,2-dichloroethane and energy consumption for evaporation of 1,2-dichloroethane in. the first tank 7. To this end, the level of liquid 1,2-dichloroethane in the second tank 6 and starting from is measured using a known device (LIC). of this measured value as a controlled parameter, the required amount of boiler feedwater under a pressure of 2.5 MPa as a cooling agent is fed into the heat exchanger 5 through a pipeline. For cooling, 180 dm of boiler feedwater is required, which in this case heats up to 100 and leaves the heat exchanger 5 through the pipeline. The amount of regenerated energy is 73.5 kJ / kg vinyl chloride.
Cooled. Up to 195 with 1,2-dichloroethane is fed through a loop of a pipeline with evenly distributed openings.
mi into the second tank 6 and mixed there with a hotter 1,2-dichloroethane, which lifts the second container from the first tank through pipes 8 into the second container, and a part of this 1,2-dichloroethane is drawn in.
The temperature in the lifting pipes, 8 is equal, and in the pipes 9, leading down, -. The amount of circulating between the first 7 and second 6 tanks of liquid 1,2-dichloroethane is equal to 9734 kg / h. For every 100 kg / h circulating between the first
7 and the second 6 tanks of liquid 1,2-dichloroethane to the second tank 6 through the pipeline feed 8.1 kg / h of fresh liquid 1,2-dichloroethane.
Vtarenny 1,2-dichloroethane at 262 ° C, freed from liquid or solid components, is introduced through a pipeline into the lower part of the convective zone 3 of the pyrolysis oven and overheated there approximately. From there it is transferred through a pipeline to the radiation zone 4 and is heated to
During gas overheating to 525 ° C, a part of 1,2-dichloroethane is split into vinyl chloride and hydrogen chloride. The hot pyrolysis gases are fed to the first tank 7 via conduit 12 and they exit this tank at 268 ° C. The average cooling rate of the pyrolysis gases in the first tank 7 is 41.5 o / s, which is 1 / 12.6 of the inlet temperature () per second. Through the pipeline, these pyrolysis gases are fed to further cooling (not shown). and they partially condense. From the thermal decomposition of the mixture of substances according to a known method, hydrogen chloride is separated in a column (not shown) at a temperature of -24 ° C. The pressure at the top of this column is set in such a way that the temperature of the gaseous evaporated 1,2-dichloroethane at the outlet of the second tank 6 is.
In this tank, 1,2-dichloroethane is evaporated at a pressure of 3.5 MPa, at a rate of 761 kg / h, which corresponds to
7.8 kg / h for every 100 kg / h of liquid 1,2-dichloroethane circulating between the first 7 and second 6 tanks. With every square meter of surface located in the second tank 6 liquid | bones (it is assumed that it is at rest) evaporation
0
five
0
five
Q g
2726 kg / h of 1,2-dichloroethane. The lower part of the first vessel 7 discharges 24 kg / h of liquid 1,2-dichloroethane, which is directed through a pipeline into a column (not shown), from the upper part of which 1,2-dichloroethane is distilled. The amount of 1,2-dichloroethane discharged from the first tank 7 is 3.0 kg / h per 100 kg / h of fresh 1,2-dichloroethane fed to the second tank 6. The average residence time of 1,2-dichloroethane in the first and the second tank is 48 minutes. In the burner 11 in the pyrolysis furnace, the pipeline feeds 0.071 nm of fuel (methane) per 1 kg of vinyl chloride produced. In the upper part of the convective zone 3 of the pyrolysis furnace, pipeline 15 supplies 110 kg / h of boiler feedwater at 100 ° C, which is heated to. The amount of energy utilized here is 45.5 kDK / kg of vinyl chloride. The pipeline discharges 290 hot water at. The amount of energy utilized in this case is 119 g-Tzh / kg vinsht chloride. The degree of cleaved chloroethane in the radiation zon of the roll oven is 65%, and the release of vinyl chloride is 312 kg / h.
1,2-dm 4 p.
After 9 months of operation, the heat exchange between the hot vinyl chloride-containing gases from the pyrolysis furnace and the liquid 1,2-dichloroethane in the first tank 7 remains almost unchanged. The temperature difference between the hot gases from the pyrolysis furnace, which. through the pipeline is withdrawn from the first vessel 7, and 1,2-g1 gas, chlorine ethane, which leaves the second vessel 6 and is fed through the pipeline into the pyrolysis furnace, is. On the heat exchange surfaces, neither on the side of hot pyrolysis gases, nor on the side of the liquid 1,2-dichloroethane, there is any noticeable increase in the years.
The energy recovered from the flue gases of the pyrolysis furnace by generating hot water is 119 kJ / kg vinyl chloride, which corresponds to a fuel consumption (methane) of 0.003 vinyl chloride. Thereby, the effective consumption of combustible gas is reduced to 0.068 HMVKr of hydrochloride, which is only 66.4% of the consumption (100%) with comparative experience. Energy saving is 33.6% with an increase in the degree of cleavage in the range of 55-65% and an increase in the service life of the pyrolysis furnace by 6 to 9 months. From the collector, 785 kg / h of 1,2-dichloroethane is withdrawn with and with the help of pumps at a pressure of 1.3 MPa and at 100 C is fed into the middle part of the convective zone of the pyrolysis furnace. Waste - from the radiation zone of the pyrolysis furnace with flue gases, liquid 1,2-dichloroethane is heated to. In tep10
of the first tank 7 1,2-dich, Porethan per 100 kg / h of fresh 1,2-dichloroethane fed to the second tank 6. The average residence time of 1,2-dichlorosthane in the first and second tanks in total was em 48 min
In the burner 11 in the pyrolysis furnace, the pipeline feeds 0.071 fuel (methane) per 1 kg of vinyl chloride produced. In x: the middle part of the convective zone of the pyrolysis furnace is fed through the pipeline 352 kg / h of nutrient
The exchanger 5 is provided with equalizing water at which the intake is between the energy transferred in the zone to liquid 1,2-dichloroethane and the energy necessary for evaporation of 1,2-dichloroethane in the first tank 7..
For this purpose, the level of liquid 1,2-dichloroethane in the second tank 6 is determined with the help of a known device 20 (tle) and the obtained value is used as an adjustable value to determine the required 25 quantity of boiler feed water supplied as a refrigerant under pressure 2, 5 MPa in the heat exchanger 5 through the pipeline. 180 dm of such water is required for cooling, which in this case is heated by 100-130 ° C. The amount of energy utilized at the same time is 73.5 kJ / kg vinyl chloride
here it is heated up.
The amount of energy utilized in this case is 145.6 kg. Kg / kg of vinyl chloride. The pipeline discharges 532 hot water with a temperature of 130 C. The amount of energy utilized in this case is 218 kJ / kg vinyl chloride. The degree of conversion in the splitting of 1,2-dichloroethane in the radiation zone -4 of the pyrolysis furnace is 65%. The amount of vinyl chloride produced is 311.3 kg / h.
After 9 months of operation, the heat transfer in the first tank 7 from the gases containing hot vinyl chloride from the pyrolysis furnace to the liquid 1,2-dichloroethane remained almost the same as at the beginning.
Flow rate circulating between the first
Cooled to about 1.2 to 7 and the second with 6 tanks of liquid 1,2-dichloroethane along the loop of the dichloroethane pipe, is 8439 kg / h, evenly distributed holes - For every 100 kg / h, each one is fed to the second tank 6, where between the first 7 and second 6 tanks, it is mixed with more hot 1,2-di-1,2-dichloroethane in the second tank 6 with chloroethane, rising from here, 0 through the pipeline, 9.3 kg / h of the first tank 7 is fed through pipes 8, with a portion of the 1,2-dichloroethane evaporating. The temperature in the lifting pipes 8 is equal to 197 ° C, and in the pipes 9 leading down -
fresh liquid 1,2-dichloroethane. The evaporated 1,2-dichloroethane, which does not contain liquid or solid components, is fed 193 ° C through a pipeline. The calculated amount of cir-45 in the lower part of the convective zone of the heating between the first 7 and second 6 volcanoes is overheated to liquid containers. 1,2-dichloroethane is 8439 kg / h. From every square meter of the surface of the liquid in the second tank 6 (it is assumed that it is in the active state) 2,723 kg / h evaporate
mH - i- i 4-. 1 CJ-i l
300 s From here it is by pipeline by 50
given to the zone is radiated and where it overheats to.
In the process of overheating the gas to 500 sec., A part of 1,2-dichloroethane is decomposed to form vinyl chloride and hydrogen chloride. The hot reaction gases are piped to the first
1,2-dichloroethane.
From the bottom of the first tank 7
25 kg / h of liquid 1,2-dichloro is discharged. tank 7, from where they come out with ethane and through a pipeline, is fed into a coil of 220 ° C. The average cooling rate is a liquor, from the upper part of which 1,2-dichlorochtan is distilled. This amount corresponds to 3.2 kg / h
the reaction gases in the first tank 7 is 44 ,, which corresponds to 1 / 11.8 of the inlet teparaty
of the first tank 7 1,2-dich, Porethan per 100 kg / h of fresh 1,2-dichloroethane fed to the second tank 6. The average residence time of 1,2-dichlorosthane in the first and second tanks in total was em 48 min
In the burner 11 in the pyrolysis furnace, the pipeline feeds 0.071 fuel (methane) per 1 kg of vinyl chloride produced. In x: the middle part of the convective zone of the pyrolysis furnace is fed through the pipeline 352 kg / h of nutrient
boiler water at, which boiling water at, which is heated here before.
The amount of energy utilized in this case is 145.6 kg. Kg / kg of vinyl chloride. The pipeline discharges 532 hot water with a temperature of 130 C. The amount of energy utilized in this case is 218 kJ / kg vinyl chloride. The degree of conversion in the splitting of 1,2-dichloroethane in the radiation zone -4 of the pyrolysis furnace is 65%. The amount of vinyl chloride produced is 311.3 kg / h.
After 9 months of operation, the heat transfer in the first tank 7 from the gases containing hot vinyl chloride from the pyrolysis furnace to the liquid 1,2-dichloroethane remained almost the same as at the beginning.
Flow rate circulating between the first
7 and the second 6 tanks of liquid 1,2-dichloroethane is 8439 kg / h. For every 100 kg / h, the discharge between the first 7 and second 6 tanks of 1,2-dichloroethane to the second tank 6 is fed through 9.3 kg. / h
fresh liquid 1,2-dichloroethane. The evaporated 1,2-dichloroethane, which does not contain liquid or solid components, is fed through the pipeline to the lower part of the convection zone of the pyrotechnic furnace and is superheated there.
mH - i- i 4-. 1 CJ-i l
300 s From here he piped by
given to the zone is radiated and where it overheats to.
In the process of overheating the gas to 500 sec., A part of 1,2-dichloroethane is decomposed to form vinyl chloride and hydrogen chloride. The hot reaction gases are piped to the first
tank 7, from where they come out at 220 C. Medium cooling rate
tank 7, from where they come out at 220 C. Medium cooling rate
the reaction gases in the first tank is 44 ,, which corresponds to 1 / 11.8 of the input terapies
ten
(500 C) in 1 s. Through the pipeline, the reaction gases are directed to a further cooling, which is carried out in a known manner, and they partially condense. The mixture of substances formed during thermal decomposition is separated in a known manner in a column from hydrogen chloride at a temperature in the upper part of the column. The pressure in the upper part of this column is set so (0.6 MPa) that the evaporated gaseous 1,2-dichloroethane leaves the second tank 6 at. In this capacity, at a pressure of 1.2 MPa, 760 kg / h of 1,2-dichloroethane is evaporated, which corresponds to 9.0 kg / h of evaporated 1,2-dichloroethane for every 1.00 kg / h of liquid 1,2-dichloroethane circulating 20 between the first 7 and second 6 tanks. The temperatures between the hot gases from the pyrolysis furnace, which are removed through the pipeline from the first tanks 7, and the gaseous 1,2-dichloro-25 ethane, which leaves the second tank 6 and are fed through the pipeline into the pyrolysis furnace. . No deposition of noticeable amounts of sediment was detected on the heat exchange surfaces either on the side of the hot reaction gases or on the ZO side of the liquid 1,2-dichloroethane.

权利要求:
Claims (2)
[1]
1. A method of producing vinyl chloride by thermal cleavage of chlorine hydrogen from 1,2-dichloroethane in a pyrolysis furnace, including indirect heating of liquid 1,2-dichloroethane in an additional capacity with hot vinyl chloride-containing gas with a temperature of 500-533 C, formed in the pyrolysis of the furnace using the heat of this gas, the evaporation of 1,2-dichloroethane and the introduction of gaseous T, 2-dichloroethane into a pyrolysis furnace, characterized in that, in order to remove the degree of cleavage of 1,2-dichloro ethane and reduce energy consumption, heat the liquid 1 , 2-dichloroethane in additional container and lead to t97-270 until it boils, boiling 1,2-dichloro ethane translates into a second tank, which, without further heating, at a pressure of 1.2-3.7 m11a, evaporates 6.0-9.0 kg / h 1,2-dichloroethane per 100 kg / h of it, circulating in their tanks, evaporated 1, ethane is fed to the pyrolysis furnace, and not the steamed 1,2-dichloroethane is returned from the second to an additional container, and fresh liquid 1, 2-dichloroethane is preheated by flue gases in the convective zone of the pyrolysis furnace or in the heat exchanger up to 150 - and then injected into the second one in an amount of 6.25-9.3 kg / h into the calculation
Liva is reduced to 0.066 vinyl-to kg / h circulating in both
chloride, which is only 64.4% of the amount of gaseous fuel (100%) that is used in comparative experience. As a result, save
a tank of 1,2-dichloroethane, and for every 100 kg / h of fresh fresh 1,2-dichl ethane injected from an additional tank, you can remove 3.0-3.6 kg / h of liquid 1,2-dichloro
energy is 35.6% while simultaneously forming with the resulting increase in the degree of cleavage by 55-65% and increasing the duration of the pyrolysis furnace by 6-9 months.
Thus, the proposed JQ method (table) significantly improves the degree of cleavage of the starting 1,2-dichloroethane and reduces energy consumption. At the same time, the proposed method can be obtained by 29.5% less re-distilled dichloroethane, thereby achieving energy savings. The purity of the obtained vinyl chloride in relation to 55
the process of evaporation by impurities and sent to the stage of separation of pure 1,2-d chloroitane.
[2]
2. The method according to claim 1, about tl and h and y and the fact that fresh liquid 1,2-dichloroethane is fed to the second tank, the temperature of which is controlled by means of thermostating means depending on the height of the liquid level in the second tank.
Priority featured
10.10.86 under item 1. 10.02.87 under item 2.
0
5 0 5
it contains butadiene, which adversely affects the polymerization process, in the proposed method is higher than in the known. Invention Formula
1. A method of producing vinyl chloride by thermally removing hydrogen chloride from 1,2-dichloroethane in a pyrolysis furnace, including indirect heating of liquid 1,2-dichloroethane in an additional container with a hot vinyl chloride-containing gas with a temperature of 500-533 ° C, which is formed in a pyrolysis furnace , using the heat of this gas, the evaporation of 1,2-dichloroethane and the introduction of gaseous T, 2-dichloroethane into a pyrolysis furnace, characterized in that, in order to increase the degree of cleavage of 1,2-dichloroethane and reduce energy consumption, heating the liquid 1, 2-dichloroethane in d The additional tank is brought to t97-270 0 - before its boiling, boiling 1,2-dichloroethane is transferred to the second tank, in which 6.0-9.0 is evaporated without further heating at a pressure of 1.2-3.7 m11a kg / h of 1,2-dichloroethane per 100 kg / h of it, circulating in both tanks, evaporated 1, ethane is fed to the pyrolysis furnace, and non-evaporated 1,2-dichloroethane is returned from the second to an additional container, and fresh liquid 1 , 2-dichloroethane is preheated with flue gases in the convection zone of the pyrolysis furnace or in the heat exchanger up to 150 - and then introduced into the second capacitively in an amount of 6,25-9,3 kg / h per
  kg / h circulating in both
  kg / h circulating in both
capacity of 1,2-dichloroethane, and for every 100 kg / h of fresh fresh 1,2-dichloroethane injected from the additional tank, 3.0-3.6 kg / h of liquid 1,2-dichlorine 45 are removed together with those formed in the proJQ
five
The process of evaporation by impurities and sent to the stage of the release of pure 1,2-dichloroitane.
2. The method according to p. 1, about tl and h and yu and so that in the second tank serves fresh liquid 1,2-dichloroethane,. the temperature of which is regulated by means of thermostatic means depending on the height of the liquid level in the second tank.
Priority featured
10.10.86 under item 1. 10.02.87 under item 2.
The amount of vinyl chloride per 36 months:
kg
7,
The amount of dichloroethane circulating in the circuit for 36 months: kg
The content of butadiene in vinyl chloride, ppm (wt.%) The content of methyl chloride vinyl chloride, ppm (wt.%)

10,231.4
98.96 13300.8
262,128-10,100
339,437-10 129.5
32400 0.35 25520 323.417-10 77.9
five
40
f2 (A
 V
/
Y VK N
L
% city /
Vt
L
YU
Y-OV FigZ
lit

类似技术:

---

公开号 | 公开日 | 专利标题

---

SU1598862A3|1990-10-07|Method of producing vinylchloride

---

RU2323199C2|2008-04-27|1,2-dichloroethane thermal cracking-mediated production of vinyl chloride

---

GB1454049A|1976-10-27|Distillation processes

---

US4788357A|1988-11-29|Vinyl chloride production

---

SU1665874A3|1991-07-23|Method of producing vinyl chloride

---

US2165100A|1939-07-04|Process for purifying phosphoric acid

---

US3425477A|1969-02-04|Method for heat recovery in evaporating and burning spent liquor

---

US4017277A|1977-04-12|Direct contact water heating system and process

---

US2898384A|1959-08-04|Process for the thermal chlorination of hydrocarbons

---

RU1773258C|1992-10-30|Method of vinyl chloride synthesis

---

US4267031A|1981-05-12|Coking process

---

US3725491A|1973-04-03|Process for recovering heat from gas mixtures obtained by the thermal cracking of hydrocarbons

---

US4645656A|1987-02-24|Process and apparatus for the production of ammonium nitrate

---

EP0200786B1|1990-01-17|Coking apparatus

---

US3282652A|1966-11-01|Apparatus for pyrolysis of dichloroethane

---

SU1749178A1|1992-07-23|Method for contact heating of water

---

JPH10279953A|1998-10-20|Apparatus for converting waste plastic into oil

---

PL111015B1|1980-08-30|Process for vinyl chloride manufacture

---

GB2179938A|1987-03-18|Production of monomeric vinyl chloride

---

CA1155416A|1983-10-18|Process for distilling crude tall oil

---

SU1616980A1|1990-12-30|Method of purifying spent oils from water and lightweight fractions

---

CN111153457A|2020-05-15|Trichloroethylene device waste liquid treatment process and equipment thereof

---

EA002895B1|2002-10-31|Method for making a hydrazine by hydrolysing an azine

---

CN107573207A|2018-01-12|A kind of Joint Production system and method for vinyl chloride

---

GB2142420A|1985-01-16|De-aeration of water

同族专利:

---

公开号 | 公开日

---

JPS6396141A|1988-04-27|

---

GR3001227T3|1992-07-30|

---

FI84471C|1991-12-10|

---

PL156507B1|1992-03-31|

---

IN170264B|1992-03-07|

---

FI874428A|1988-04-11|

---

JP2509637B2|1996-06-26|

---

MX169575B|1993-07-13|

---

AU599152B2|1990-07-12|

---

PL268146A1|1988-12-08|

---

AR247376A1|1994-12-29|

---

EP0264065A1|1988-04-20|

---

BR8705418A|1988-05-24|

---

NO874236L|1988-04-11|

---

HU202175B|1991-02-28|

---

US4798914A|1989-01-17|

---

HUT44996A|1988-05-30|

---

DE3704028A1|1988-04-14|

---

DE3765221D1|1990-10-31|

---

FI84471B|1991-08-30|

---

ES2018526B3|1991-04-16|

---

FI874428A0|1987-10-08|

---

CA1300645C|1992-05-12|

---

NO165876C|1991-04-24|

---

NO874236D0|1987-10-09|

---

AU7950087A|1988-04-14|

---

NO165876B|1991-01-14|

---

EP0264065B1|1990-09-26|

引用文献:

---

公开号 | 申请日 | 公开日 | 申请人 | 专利标题

---

---

DE2313037C3|1973-03-16|1986-06-19|Hoechst Ag, 6230 Frankfurt|Process for the production of vinyl chloride by the thermal cleavage of 1,2-dichloroethane|

---

EP0014920B1|1979-02-23|1982-12-08|Hoechst Aktiengesellschaft|Process for the recovery of pyrolysis energy in the preparation of vinyl chloride by incomplete thermal splitting of 1,2-dichloroethane|

---

DE3440685A1|1984-11-07|1986-05-07|Wacker-Chemie GmbH, 8000 München|METHOD FOR PRODUCING VINYL CHLORIDE BY THERMAL CLEAVING OF PURIFIED 1,2-DICHLORETHANE|

---

DE3543222A1|1985-12-06|1987-06-11|Wacker Chemie Gmbh|IMPROVED METHOD FOR PRODUCING VINYL CHORIDE BY THERMAL CLEAVING 1,2-DICHLORETHANE|DE3718317A1|1986-12-10|1988-06-16|Bayer Ag|SUBSTITUTED BASIC 2-AMINOTETRALINE|

---

DE19859262A1|1998-12-22|2000-07-06|Krupp Uhde Gmbh|Process for the evaporation of 1,2-dichloroethane |

---

DE10219723B4|2002-05-02|2005-06-09|Uhde Gmbh|Process for the preparation of unsaturated halogen-containing hydrocarbons and device suitable therefor|

---

TWI327995B|2003-04-11|2010-08-01|Vinnolit Gmbh & Co Kg|Vorrichtung und verfahren zur herstellung von vinylchlorid durch thermische spaltung von 1,2-dichlorethan|

---

DE10319811A1|2003-04-30|2004-11-18|Uhde Gmbh|Device for coupling electromagnetic radiation into a reactor and reactor containing this device|

---

DE102008049262B4|2008-09-26|2016-03-17|Thyssenkrupp Industrial Solutions Ag|Process and apparatus for the preparation of ethylenically unsaturated halogenated hydrocarbons|

---

DE102008049261B4|2008-09-26|2018-03-22|Thyssenkrupp Industrial Solutions Ag|Process and apparatus for the preparation of ethylenically unsaturated halogenated hydrocarbons|

---

DE102008049260B4|2008-09-26|2016-03-10|Thyssenkrupp Industrial Solutions Ag|Process and apparatus for the preparation of ethylenically unsaturated halogenated hydrocarbons|

---

EP2867601B1|2012-06-12|2018-01-10|Shell Internationale Research Maatschappij B.V.|Apparatus and method for heating a liquefied stream|

---

US20140216067A1|2012-06-12|2014-08-07|Shell Internationale Research Maatschappij B.V.|Method and apparatus for heating a liquefied stream|

---

DE102019206155A1|2019-04-30|2020-11-05|Thyssenkrupp Ag|Process and plant for the production of vinyl chloride from 1,2-dichloroethane|

---

DE102019206154A1|2019-04-30|2020-11-05|Thyssenkrupp Ag|Process and plant for the production of vinyl chloride from 1,2-dichloroethane|

法律状态:
2007-09-20| REG| Reference to a code of a succession state|Ref country code: RU Ref legal event code: MM4A Effective date: 20041010 |

优先权:

---

申请号 | 申请日 | 专利标题

---

DE3634550|1986-10-10|

---

DE19873704028|DE3704028A1|1986-10-10|1987-02-10|METHOD FOR PRODUCING VINYL CHLORIDE BY THERMAL CLEAVING 1,2-DICHLORETHANE|

---