• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    The invention relates to methods for recovering heat from flue gas generated during the combustion of organic chloride compounds, and reduces energy losses and reduces equipment corrosion. For this, the flue gas during heat recovery and high pressure water vapor production is cooled in two successive cooling stages and then hydrogen chloride contained in the flue gas is subjected to processing in the third cooling stage.
    公开号:SU1667639A3
    申请号:SU853925750
    申请日:1985-07-04
    公开日:1991-07-30
    发明作者:Думмер Герхард；Шмидхаммер Лудвиг；Хиршманн Петер；Штеттнер Герхард
    申请人:Вакер-Хеми Гмбх (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to a method of heat recovery of flue gas obtained by burning organic chloride compounds at 900-1300 ° C and a pressure of 0.9-1.5 abs. Bar, the flue gas being cooled during the heat recovery process, and the hydrogen chloride produced is processed.
    The purpose of the invention is to reduce energy loss and reduce equipment corrosion.
    The method is carried out as follows.
    Combustion should be carried out at 900-1300 ° C and a pressure of 0.9-1.5 abs. Bar with an excess of oxygen. Often, to achieve a sufficiently high calorific value of the mixture, additional fuel is burned. This fuel can be a combustible gas that feeds the supporting flame.
    The flue gas leaving the combustion chamber contains hydrogen chloride, water vapor, carbon dioxide, oxygen, nitrogen, and traces of chlorine and carbon monoxide as important components. It is first subjected to rapid cooling in the first cooling stage to 250-350 ° C with a contact time of 0.05-0.15 s. This first heat exchanger may, for example, be designed as a waste heat boiler in the form of a gas-tube boiler, in which flue gas passes through pipes and is cooled with boiling water from the annular space. Due to the favorable temperature gradient between the flue gas and the pipe wall, this heat exchanger can be made in the form of a relatively small, compact device made of unalloyed steel.
    Then the flue gas from 250-350 ° C is sent to the second heat exchanger. This heat exchanger is designed in such a way that after a contact time of 1.3-2.0 s has elapsed, the flue gas leaving the second cooling stage has a temperature of 140-160 ° C. Use
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    water as a cooling medium flows through the coolant in the direction opposite to the flue gas flow; it is supplied with a minimum temperature of 110 ° C, preferably from 120-125 ° C, and at the outlet of the cooler its temperature is 200-220 ° C. The water thus heated is fed to the first heat exchanger, at the outlet of which it is a high-pressure steam. The heat given off by the flue gas to the cooling medium in this cooling stage is converted into water evaporation energy, while the water vapor has a pressure range of 18-21 abs. Bar. This steam can be further used in any suitable way, for example for heating distillation columns and the like.
    The second cooling stage is carried out in accordance with the method parameters to be observed. Boiler structures equipped with silver-plated cooling tubes have been particularly well recommended. The flue gas passes through the annular space of the cooling device, while the cooling medium flows through in most cases in the form of cooling coils with finned pipes.
    With the observance of the parameters of the method, this cooling stage can be designed without special corrosion-resistant equipment. For example, this device may be made of unalloyed steel.
    Then, the flue gas cooled in the second stage to 140–160 ° C is heated in the third stage of processing to produce hydrochloric acid. The flue gas is cooled to a temperature below the dew point by directly cooling it with water or, if necessary, with the resulting hydrochloric acid directed along a circulating circuit. This third stage can be, for example, made in the form of a corrosion-resistant instantaneous cooling device with a scrubber connected behind it, from which the flue gas, after intensive washing, is directed to the atmosphere.
    According to the proposed method, it is possible to utilize a larger amount of heat from the flue gases arising from the burning of organic chloride compounds than has been achieved before. In addition, by reducing the volume of flue gas, condensation and rinsing processes become more efficient and less harmful to the environment.
    PRI me R 1. In the combustion chamber at 950 ° C and a pressure of 0.965 absolute bar by burning 450 standards, m / h of natural gas with an additive of 9500 standards. m3 / h of air with a duration of exposure of 1.03 s were burned:
    12,000 norms M3 / h of gaseous wastes of ethyleneoxychlorination;
    400 standards, m / h gaseous technological waste for the direct chlorination of ethylene, distillation and storage of 1.2-dichloroethane;
    300 kg / h of low boiling point gross formula C1.35H2.3CI23;
    5,900 kg / h of high-boiling substances of brutto-formula C2.1НзбС1з5;
    1500 standards, m / h of hydrogen chloride, contaminated with 0.4 mol.% Of carbon tetrachloride and 100 volume ppm of perch-lorethylene.
    The composition of the gaseous waste ethylene oxide, mol%: hydrogen chloride 2, carbon monoxide 0.5; carbon dioxide 0.7; 1.2-dichloroethane 0.15; ethyl chloride 0.25;
    5 ethylene 0.05; oxygen 20; nitrogen + argon 94.35.
    Composition of technological gaseous wastes for direct chlorination of ethylene, mol.%: Hydrogen chloride 2; 1.2-dichloro-tan 2; ethyl chloride 2; vinyl chloride 4; oxygen 5; ethylene 2; nitrogen 83.
    24348 norms, m3 of flue gas with a temperature of 950 ° C of the following composition, mol.%: Hydrogen chloride
    5 9.4; steam 4.2: carbon dioxide 4.7; oxygen 3.0; nitrogen 78.7; 200 volume ppm of chlorine, 10 volume ppm of carbon monoxide.
    The flue gas was directed to the boiler, where it is for a duration of
    0 0-15 s cooled to 320 ° C. The flue gas leaving the recovery boiler is then introduced into a second heat exchanger equipped with finned cooling coils, where it is at the contact time,
    5 equal to 1.67 s, cooled to 150 ° C. From the second heat exchanger, the flue gas entered the instantaneous cooling device, where it was cooled to a dew point temperature of 52 ° C.
    Q The amount of flue gas at the outlet of the gas exhaust pipe located behind the gas scrubber was 28,300 standards. me / h
    In the second heat exchanger filed
    5 12.3 IU of water per hour with a temperature of 120 ° C and a pressure of 20.5 bar. At the outlet of the boiler feedwater, the cooling water temperature was 213 ° C. With this temperature, water at a pressure of 20 bar was pumped into the waste heat boiler. On
    12.3 t / h of water vapor with a pressure of 19 bar abs. The total amount of steam produced was directed to the heat network of the plant.
    After two years of use in the area of the second heat exchanger, no signs of corrosion or contamination of silver pipes were found.
    Example 2 The method of operation is repeated according to Example 1 with the only difference that no additional cooling stage was installed between the recovery boiler and the instantaneous cooling device. The same amount of flue gas of the same composition was cooled in the recovery boiler. Cooling water was also supplied to the recovery boiler, however, its temperature was only 120 ° C, since there was no second heat exchanger.
    Steam production was reduced by 3 t / h to 9.3 t / s compared to the method of operation according to example 1. In addition, the flue gas reached the instantaneous cooling device with a temperature of 320 ° C, where it was cooled to a dew point temperature of 67 ° WITH. Due to the higher dew point temperature, evaporation of water has increased by approx. by 40,%, due to which the amount of flue gas at the outlet of the exhaust gas pipe after flushing increased to 31,500 standards. m3 / h
    EXAMPLE 3. Similar to Example 1, flue gas is cooled in a first cooling stage for 0.15 s to 320 ° C. Following this, it is fed to the second stage, where it is cooled for 2.0 s to
    0
    160 ° C. The resulting amount of steam was 12.0 t / h. After work, no corrosion of the equipment was observed.
    PRI me R 4. The flue gas flow, according to Example 1, is cooled in a first stage for 0.05 seconds to 300 ° C. In the second cooling stage, the flue gas flow was cooled for 1.3 seconds to 145 ° C. The resulting amount of steam was 12.4 t / h. Equipment corrosion was not observed.
    权利要求:
    Claims (1)
    [1]
    The invention of the method of heat recovery of flue gas obtained by burning organic
    chlorine compounds at 900-1300 ° C and 0.9-1.5 abs bar, which includes cooling the flue gas to produce hydrogen chloride and supplying hydrogen chloride for processing, characterized in that
    reducing energy losses and reducing equipment corrosion, cooling the flue gas is carried out in three stages, the first of which cools the gas to 250-350 ° C with a gas contact time with a heat exchange surface of 0.05-0.15 s. on the second - to a temperature not lower than 140 ° C with the time of contact of the gas with the heat exchange surface 1.3-2.0 s, and at the third stage - to the dew point temperature, with
    washing the gas after the third stage with water to obtain hydrogen chloride in the form of an aqueous solution, while in the first two stages water counter-cooling is applied with water supply at 110140 ° С to the second stage and then at 200-220 ° С the first and third steps are corrosion resistant.
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    同族专利:
    公开号 | 公开日
    JPS6260134B2|1987-12-15|
    JPS6190725A|1986-05-08|
    US4606742A|1986-08-19|
    DE3436139A1|1986-04-10|
    EP0177013A2|1986-04-09|
    DE3575081D1|1990-02-08|
    EP0177013B1|1990-01-03|
    EP0177013A3|1988-01-20|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    RU2610355C1|2015-09-25|2017-02-09|Федеральное государственное бюджетное образовательное учреждение высшего образования "Тверской государственный технический университет"|Tpp flue gases heat and condensate utilizer|US2490454A|1946-06-20|1949-12-06|Du Pont|Process for the recovery of hydrogen chloride from off-gas|
    NL68945C|1946-11-04|
    US2675890A|1949-01-25|1954-04-20|Schweizerhall Saeurefab|Process for separating chlorides from gaseous mixtures thereof|
    US2675889A|1949-04-01|1954-04-20|Schweizerhall Saeurefab|Method for processing crude gases obtained on halogenating metallic ores|
    IT951600B|1971-11-17|1973-07-10|Sir Soc Italiana Resine Spa|IMPROVEMENTS RELATING TO THE PREPARATION OF Aqueous HYDROCHLORIC ACID SOLUTIONS|
    DE2634959C2|1976-08-04|1984-09-20|Hoechst Ag, 6230 Frankfurt|Process for obtaining hydrochloric acid by removing hydrogen chloride from combustion gases|
    US4227647A|1977-05-25|1980-10-14|Leif Eriksson|Device for cooling chimney gases|DE3616333C1|1986-05-15|1987-04-16|Krantz H Gmbh & Co|Process for the thermal cleaning of exhaust gases from a heat treatment device|
    AT90224T|1989-04-17|1993-06-15|Krc Umwelttechnik Gmbh|METHOD FOR PURIFYING EXHAUST GAS WITH A HIGH CHLORIDE CONTENT.|
    AT392912B|1989-12-27|1991-07-10|Waagner Biro Ag|Method of preventing the formation of organic pollutants such as dioxin and/or furan|
    JP2694631B2|1994-02-03|1997-12-24|株式会社タステム|High temperature exhaust gas forced rapid cooling device|
    DE4406967A1|1994-03-03|1995-09-28|Erno Raumfahrttechnik Gmbh|High-temperature combustion destruction of toxic gases|
    DE102007018014A1|2007-04-17|2008-10-23|Bayer Materialscience Ag|Heat integration in a Deacon process|
    CN102418103B|2011-12-13|2013-06-05|长沙市中蓝清洗技术有限公司|Chemical for cleaning boiler|
    CN105525071B|2016-01-30|2020-03-06|青岛海德锻造有限公司|Quenching furnace capable of fully utilizing waste heat|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE19843436139|DE3436139A1|1984-10-02|1984-10-02|METHOD FOR HEAT RECOVERY IN THE COMBUSTION OF ORGANIC CHLORINE COMPOUNDS|
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