CN201762268U - Chlorohydrination reaction control system - Google Patents
Chlorohydrination reaction control system Download PDFInfo
- Publication number
- CN201762268U CN201762268U CN2010202287747U CN201020228774U CN201762268U CN 201762268 U CN201762268 U CN 201762268U CN 2010202287747 U CN2010202287747 U CN 2010202287747U CN 201020228774 U CN201020228774 U CN 201020228774U CN 201762268 U CN201762268 U CN 201762268U
- Authority
- CN
- China
- Prior art keywords
- propylene
- chlorine
- gas
- chlorohydrin
- mixed gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 30
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims abstract description 104
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims abstract description 104
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 claims abstract description 45
- 239000000463 material Substances 0.000 claims abstract description 40
- XENVCRGQTABGKY-ZHACJKMWSA-N chlorohydrin Chemical compound CC#CC#CC#CC#C\C=C\C(Cl)CO XENVCRGQTABGKY-ZHACJKMWSA-N 0.000 claims abstract description 24
- 238000011084 recovery Methods 0.000 claims abstract description 14
- MZPBNFLTHBUURE-UHFFFAOYSA-N C=CC.[Cl] Chemical group C=CC.[Cl] MZPBNFLTHBUURE-UHFFFAOYSA-N 0.000 claims abstract description 13
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims description 26
- 239000000460 chlorine Substances 0.000 claims description 26
- 229910052801 chlorine Inorganic materials 0.000 claims description 26
- 230000001105 regulatory effect Effects 0.000 claims description 16
- 238000000034 method Methods 0.000 claims description 10
- 239000000203 mixture Substances 0.000 claims description 7
- AKHNMLFCWUSKQB-UHFFFAOYSA-L sodium thiosulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=S AKHNMLFCWUSKQB-UHFFFAOYSA-L 0.000 claims description 4
- 230000001276 controlling effect Effects 0.000 claims 1
- RZWHKKIXMPLQEM-UHFFFAOYSA-N 1-chloropropan-1-ol Chemical compound CCC(O)Cl RZWHKKIXMPLQEM-UHFFFAOYSA-N 0.000 abstract description 18
- 238000007086 side reaction Methods 0.000 abstract description 8
- 239000000376 reactant Substances 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 52
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- KNKRKFALVUDBJE-UHFFFAOYSA-N 1,2-dichloropropane Chemical group CC(Cl)CCl KNKRKFALVUDBJE-UHFFFAOYSA-N 0.000 description 3
- 239000003513 alkali Substances 0.000 description 3
- QWPPOHNGKGFGJK-UHFFFAOYSA-N hypochlorous acid Chemical compound ClO QWPPOHNGKGFGJK-UHFFFAOYSA-N 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- GOOHAUXETOMSMM-UHFFFAOYSA-N Propylene oxide Chemical compound CC1CO1 GOOHAUXETOMSMM-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 150000003945 chlorohydrins Chemical group 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- GVNVAWHJIKLAGL-UHFFFAOYSA-N 2-(cyclohexen-1-yl)cyclohexan-1-one Chemical compound O=C1CCCCC1C1=CCCCC1 GVNVAWHJIKLAGL-UHFFFAOYSA-N 0.000 description 1
- 101150065749 Churc1 gene Proteins 0.000 description 1
- 102100038239 Protein Churchill Human genes 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 238000007127 saponification reaction Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
本实用新型公开一种氯醇化反应控制系统，主要是为了减少副反应的发生，提高氯醇化反应物氯丙醇的产出率而设计。包括丙烯蒸发器、氯气预溶器、氯醇反应器、丙烯回收塔和氯丙醇分离器，所述氯醇反应器的物料输入端分别与所述丙烯蒸发器的物料输出端、所述氯气预溶器的物料输出端和所述丙烯回收塔的物料输出端相连通，所述氯醇反应器的物料输出端与所述氯丙醇分离器的物料输入端相连通，在所述丙烯蒸发器和所述氯醇反应器之间，所述氯气预溶器的物料输入端设置一氯气—丙烯比值调节系统。本实用新型根据反应氯气的流量调节丙烯混合气的流量，使得丙烯混合气与氯气的摩尔比保持在1.6～1.7，提高氯丙醇的产出率，减少副反应的发生。
The utility model discloses a chlorohydrinization reaction control system, which is mainly designed for reducing the occurrence of side reactions and increasing the output rate of chlorohydrinization reactant chloropropanol. Comprising a propylene evaporator, a chlorine gas predissolver, a chlorohydrin reactor, a propylene recovery tower and a chloropropanol separator, the material input end of the chlorohydrin reactor is respectively connected with the material output end of the propylene evaporator, the chlorine gas The material output end of the predissolver is connected with the material output end of the propylene recovery tower, the material output end of the chlorohydrin reactor is connected with the material input end of the chloropropanol separator, and the propylene evaporates Between the reactor and the chlorohydrin reactor, a chlorine-propylene ratio adjustment system is arranged at the material input end of the chlorine gas predissolver. The utility model adjusts the flow rate of the propylene mixed gas according to the flow rate of the reactive chlorine gas, so that the molar ratio of the propylene mixed gas to the chlorine gas is maintained at 1.6-1.7, improves the output rate of chloropropanol, and reduces the occurrence of side reactions.
Description
技术领域technical field
本实用新型涉及一种化工生产领域，尤其是一种环氧丙烷生产控制系统。The utility model relates to the field of chemical production, in particular to a production control system for propylene oxide.
背景技术Background technique
丙烯和氯气是生产环氧丙烷的主要原料，进行氯醇化反应时，水、丙烯和氯气进入反应器进行化学反应，生成氯丙醇，这是主反应过程。同时还会发生丙烯和氯气直接发生化学反应的副反应过程，副反应生成物是二氯丙烷。因为二氯丙烷能够溶解丙烯，降低主反应中丙烯量，并且副反应也消耗大量丙烯和氯气。所以，氯气在反应前，首先要经过氯气预溶器，气态氯溶于工艺水中，在水中充分溶解，生成次氯酸，溶解了大量氯气的“氯水”送入氯醇反应器，与丙烯发生反应，避免氯气与丙烯直接接触生成二氯丙烷。Propylene and chlorine gas are the main raw materials for the production of propylene oxide. During the chloroalcoholization reaction, water, propylene and chlorine gas enter the reactor for a chemical reaction to produce chloropropanol, which is the main reaction process. Simultaneously, the side reaction process of direct chemical reaction between propylene and chlorine will occur, and the side reaction product is dichloropropane. Because dichloropropane can dissolve propylene, reduce the amount of propylene in the main reaction, and the side reaction also consumes a large amount of propylene and chlorine. Therefore, before the reaction of chlorine gas, it must first pass through the chlorine gas pre-dissolver. The gaseous chlorine is dissolved in the process water, fully dissolved in the water to generate hypochlorous acid, and the "chlorine water" with a large amount of chlorine dissolved is sent to the chlorohydrin reactor. Reaction occurs, to avoid direct contact between chlorine and propylene to generate dichloropropane.
为了保证溶氯效果，一般要求氯气稍微过量，但氯气量大了以后，会加大副反应物的生成量；同样，进入氯醇化反应器的气化丙烯量少，会降低反应速度；丙烯量增多，会加剧副反应。为了尽量减少副反应及其产物，丙烯、氯气的配比是氯醇化反应中最为重要的工艺参数，直接决定着中间产物氯丙醇的产出率。In order to ensure the effect of dissolving chlorine, a slight excess of chlorine gas is generally required, but when the amount of chlorine gas is large, the amount of by-products generated will be increased; similarly, the amount of gasified propylene entering the chloroalcoholation reactor is small, which will reduce the reaction speed; the amount of propylene Increase, will exacerbate side effects. In order to minimize side reactions and their products, the ratio of propylene and chlorine is the most important process parameter in the chlorohydrination reaction, which directly determines the output rate of the intermediate product chloropropanol.
实用新型内容Utility model content
本实用新型的主要目的就是提供一种能够有效减少副反应，提高氯丙醇的产出率的氯醇化反应控制系统。The main purpose of the utility model is to provide a chlorohydrination reaction control system that can effectively reduce side reactions and improve the output rate of chloropropanol.
本实用新型提供的一种氯醇化反应控制系统，包括：A kind of chlorohydrination reaction control system provided by the utility model comprises:
包括丙烯蒸发器、氯气预溶器、氯醇反应器、丙烯回收塔和氯丙醇分离器，所述氯醇反应器的物料输入端分别与所述丙烯蒸发器的物料输出端、所述氯气预溶器的物料输出端和所述丙烯回收塔的物料输出端相连通，所述氯醇反应器的物料输出端与所述氯丙醇分离器的物料输入端相连通，在所述丙烯蒸发器和所述氯醇反应器之间，所述氯气预溶器的物料输入端设置一氯气—丙烯比值调节系统，所述的氯气—丙烯比值调节系统设置有两个进气端口和两个出气端口，其中，第一进气端口与所述丙烯蒸发器的物料输出端和所述丙烯回收塔的物料输出端相连通，第二进气端口外接氯气，第一出气端口与所述氯醇反应器的物料输入端连接，第二出气端口与所述氯气预溶器的物料输入端连接。Comprising a propylene evaporator, a chlorine gas predissolver, a chlorohydrin reactor, a propylene recovery tower and a chloropropanol separator, the material input end of the chlorohydrin reactor is respectively connected with the material output end of the propylene evaporator, the chlorine gas The material output end of the predissolver is connected with the material output end of the propylene recovery tower, the material output end of the chlorohydrin reactor is connected with the material input end of the chlorohydrin separator, and the propylene evaporates Between the reactor and the chlorohydrin reactor, a chlorine-propylene ratio adjustment system is set at the material input end of the chlorine predissolver, and the chlorine-propylene ratio adjustment system is provided with two inlet ports and two gas outlets port, wherein the first air inlet port is connected with the material output end of the propylene evaporator and the material output end of the propylene recovery tower, the second air inlet port is externally connected to chlorine gas, and the first gas outlet port reacts with the chlorohydrins connected to the material input end of the chlorine gas predissolver, and the second gas outlet port is connected to the material input end of the chlorine gas predissolver.
进一步地，所述氯气—丙烯比值调节系统包括：在线分析仪，比值调节器，氯气控制回路和丙烯混合气体控制回路；其中，Further, the chlorine-propylene ratio adjustment system includes: an online analyzer, a ratio regulator, a chlorine gas control loop and a propylene mixed gas control loop; wherein,
所述在线分析仪用于分析丙烯混合气体的组分及含量；The online analyzer is used to analyze the components and content of the propylene mixed gas;
所述比值调节器用于根据所述在线分析仪的组分及含量调节所述丙烯混合气体与氯气的摩尔比维持在1.6～1.7，并根据氯气控制回路输送的流量调节所述丙烯混合气体控制回路输送丙烯混合气体的流量；The ratio regulator is used to adjust the molar ratio of the propylene mixed gas to chlorine gas at 1.6 to 1.7 according to the composition and content of the online analyzer, and adjust the propylene mixed gas control loop according to the flow rate delivered by the chlorine gas control loop The flow rate of transporting propylene mixed gas;
所述氯气控制回路包括依次连接的氯气流量调节器、氯气调节阀、氯气流量变送器；The chlorine gas control circuit comprises a chlorine gas flow regulator, a chlorine gas regulating valve, and a chlorine gas flow transmitter connected in sequence;
所述丙烯混合气控制回路包括依次连接的丙烯混合气流量调节器、丙烯调节阀、丙烯流量变送器；The propylene mixed gas control loop includes a propylene mixed gas flow regulator, a propylene regulating valve, and a propylene flow transmitter connected in sequence;
所述氯气控制回路和所述丙烯混合气控制回路经所述比值调节器连接。The chlorine gas control loop and the propylene mixture gas control loop are connected through the ratio regulator.
进一步地，所述在线分析仪设为在线工艺气相色谱分析仪。Further, the online analyzer is set as an online process gas chromatograph analyzer.
进一步地，所述氯气流量调节器设为PI调节器，所述氯气调节阀设为气动隔膜阀，所述氯气流量变送器设为差压式漩涡流量变送器。Further, the chlorine gas flow regulator is a PI regulator, the chlorine gas regulating valve is a pneumatic diaphragm valve, and the chlorine gas flow transmitter is a differential pressure vortex flow transmitter.
进一步地，丙烯混合气流量调节器设为PI调节器，丙烯调节阀气动薄膜柱塞型单座调节阀，所述丙烯流量变送器设为漩涡流量变送器。Further, the propylene mixed gas flow regulator is set as a PI regulator, the propylene regulating valve is a pneumatic film plunger type single-seat regulating valve, and the propylene flow transmitter is set as a vortex flow transmitter.
本实用新型提供的所述氯醇化反应控制系统，通过在氯醇化反应中设置一氯气—丙烯比值调节系统，使得丙烯混合气体的平均摩尔与氯气平均摩尔的之比保持在1.6-1.7，有效的减少了副反应的发生，提高了氯醇化反应物氯丙醇的产出率。The chlorohydrination reaction control system provided by the utility model, by setting a chlorine-propylene ratio adjustment system in the chlorohydrination reaction, makes the ratio of the average mole of propylene mixed gas to the average mole of chlorine gas remain at 1.6-1.7, effectively The occurrence of side reactions is reduced, and the output rate of chlorohydrin reaction product chloropropanol is improved.
附图说明Description of drawings
图1为本实用新型氯醇化反应控制系统的氯醇化反应流程图；Fig. 1 is the chlorohydrination reaction flowchart of the utility model chlorohydrination reaction control system;
图2为本实用新型氯醇化反应控制系统的氯气—丙烯比值调节系统示意图。Fig. 2 is a schematic diagram of the chlorine-propylene ratio adjustment system of the chlorohydrination reaction control system of the present invention.
具体实施方式Detailed ways
下面结合说明书附图对本实用新型的具体实施方式做详细描述。The specific embodiment of the utility model will be described in detail below in conjunction with the accompanying drawings.
如图1所示该氯醇化反应控制系统，包括丙烯蒸发器、氯气预溶器、氯醇反应器、丙烯回收塔和氯丙醇分离器，该氯醇反应器的物料输入端分别与该丙烯蒸发器的物料输出端、该氯气预溶器的物料输出端和该丙烯回收塔的物料输出端相连通，该氯醇反应器的物料输出端与该氯丙醇分离器的物料输入端相连通，在该丙烯蒸发器和该氯醇反应器之间，该氯气预溶器的物料输入端设置一氯气—丙烯比值调节系统，该的氯气—丙烯比值调节系统设置有两个进气端口和两个出气端口，其中，第一进气端口与该丙烯蒸发器的物料输出端和该丙烯回收塔的物料输出端相连通，第二进气端口外接氯气，第一出气端口与该氯醇反应器的物料输入端连接，第二出气端口与该氯气预溶器的物料输入端连接。在控制过程中，该氯气—丙烯比值调节系统是通过调节氯气和丙烯混合气(纯丙烯气体及回收的反应尾气)的流量，来控制氯气和丙烯的配比。This chlorohydrinization reaction control system as shown in Figure 1 comprises propylene evaporator, chlorine predissolver, chlorohydrin reactor, propylene recovery tower and chloropropanol separator, and the material input end of this chlorohydrin reactor is connected with this propylene respectively The material output end of the evaporator, the material output end of the chlorine predissolver and the material output end of the propylene recovery tower are connected, the material output end of the chlorohydrin reactor is connected with the material input end of the chloropropanol separator , between the propylene evaporator and the chlorohydrin reactor, a chlorine-propylene ratio adjustment system is set at the material input end of the chlorine pre-dissolver, and the chlorine-propylene ratio adjustment system is provided with two inlet ports and two A gas outlet port, wherein, the first gas inlet port is connected with the material output end of the propylene evaporator and the material output end of the propylene recovery tower, the second gas inlet port is externally connected with chlorine gas, and the first gas outlet port is connected with the chlorohydrin reactor The material input end of the chlorine gas predissolver is connected, and the second gas outlet port is connected with the material input end of the chlorine gas predissolver. During the control process, the chlorine-propylene ratio adjustment system controls the ratio of chlorine and propylene by adjusting the flow rate of the mixed gas of chlorine and propylene (pure propylene gas and recovered reaction tail gas).
丙烯从丙烯球罐管道输送到丙烯蒸发器，汽化后通过调节气体压力，与回收丙烯混合形成丙烯混合气，该丙烯混合气和外接氯气经该氯气—丙烯比值调节系统，根据氯气的流量调节丙烯混合气的流量，使得丙烯混合气与氯气的摩尔比保持在1.6-1.7。经该氯气—丙烯比值调节系统输出的氯气进入该氯气预溶器溶解后进入该氯醇化反应器，同时输出的该丙烯混合气进入该氯醇化反应器，并发生氯醇化反应，反应式为：Propylene is transported from the propylene spherical tank to the propylene evaporator. After vaporization, the gas pressure is adjusted and mixed with recovered propylene to form a propylene mixed gas. The propylene mixed gas and the external chlorine gas pass through the chlorine-propylene ratio adjustment system to adjust the propylene according to the flow rate of the chlorine gas. The flow rate of the mixed gas makes the mol ratio of the propylene mixed gas to the chlorine gas remain at 1.6-1.7. The chlorine gas output by the chlorine-propylene ratio adjustment system enters the chlorine predissolver for dissolution and enters the chloroalcoholization reactor, and the propylene mixed gas output at the same time enters the chloroalcoholation reactor, and the chloroalcoholation reaction occurs, and the reaction formula is:
CL2+H2O→HCLO(次氯酸)+HCLCL 2 +H 2 O→HCLO (hypochlorous acid)+HCL
CH3CHCH2+HCLO(次氯酸)→CH3CHOHCH2CL(β_氯丙醇)+CH3CHCLCH2OH(α_氯丙醇)CH 3 CHCH 2 +HCLO(hypochlorous acid)→CH 3 CHOHCH 2 CL(β_chloropropanol)+CH 3 CHCLCH 2 OH(α_chloropropanol)
反应生成的氯丙醇水溶液进入氯丙醇分离器进行气液分离，氯丙醇溶液从氯丙醇分离器底部进入氯丙醇缓冲罐，供皂化工序使用。另外，氯醇反应器的反应尾气进入第一碱洗塔，洗去酸雾，然后将气体冷却。冷却下来的气体大部分进入丙烯回收塔，回收的丙烯与新鲜丙烯再次混合。冷却下来的液体和丙烯回收塔回收丙烯以后的气体进入碱液循环罐。经丙烯回收塔回收丙烯以后的气体，主要是不发生反应的丙烷、氧气、氮气等惰性气体，还有少量过量的丙烯，从第二碱洗塔的底部进入，碱洗酸雾和可能带出的氯气后，经冷却、气液分离，排空。The chloropropanol aqueous solution generated by the reaction enters the chloropropanol separator for gas-liquid separation, and the chloropropanol solution enters the chloropropanol buffer tank from the bottom of the chloropropanol separator for use in the saponification process. In addition, the reaction tail gas of the chlorohydrin reactor enters the first alkali washing tower to wash away the acid mist, and then the gas is cooled. Most of the cooled gas enters the propylene recovery tower, and the recovered propylene is mixed with fresh propylene again. The cooled liquid and the gas after recovering propylene from the propylene recovery tower enter the lye circulation tank. The gas after propylene is recovered by the propylene recovery tower is mainly inert gases such as propane, oxygen and nitrogen that do not react, and a small amount of excess propylene, which enters from the bottom of the second alkali washing tower, and the acid mist and may be brought out by the alkali washing After the chlorine gas is released, it is cooled, separated from gas and liquid, and emptied.
如图2所示该氯醇化反应控制系统，该的氯气—丙烯比值调节系统包括：在线分析仪，比值调节器，氯气控制回路和丙烯混合气控制回路；其中，This chlorohydrinization reaction control system as shown in Figure 2, this chlorine-propylene ratio adjustment system comprises: on-line analyzer, ratio regulator, chlorine control loop and propylene mixed gas control loop; Wherein,
该在线分析仪用于分析丙烯混合气体的组分及含量；可选用日本横河公司出产的GC8型工艺气相色谱仪，对丙烯混合气体组份进行在线分析。丙烯混合气经GC8型工艺气相色谱仪分析出丙烯混合气组分数据(丙烯、丙烷、氢气、氧气及其他气体)并计算出丙烯混合气体的平均分子量。The on-line analyzer is used to analyze the components and content of the propylene mixed gas; the GC8 process gas chromatograph produced by Yokogawa Corporation of Japan can be used for online analysis of the propylene mixed gas components. The propylene mixture gas is analyzed by the GC8 process gas chromatograph to obtain the propylene mixture gas component data (propylene, propane, hydrogen, oxygen and other gases) and calculate the average molecular weight of the propylene mixture gas.
该比值调节器用于根据该在线分析仪的组分及含量调节该丙烯混合气与氯气的摩尔质量比维持在1∶1.7，并控制氯气控制回路输送的流量与该丙烯混合气控制回路输送丙烯混合气的流量比为1.6～1.7；The ratio regulator is used to adjust the molar mass ratio of the propylene mixed gas to chlorine gas according to the composition and content of the online analyzer to maintain at 1:1.7, and to control the flow rate delivered by the chlorine gas control loop to mix with the propylene mixed gas control loop delivered by the propylene mixed gas The gas flow ratio is 1.6 to 1.7;
该氯气控制回路包括依次连接的氯气流量调节器、调节阀、氯气流量变送器；该氯气调节器选用PI调节规律，氯气流量变送器选用差压式漩涡流量变送器，氯气调节阀选用气动隔膜阀。较佳的，对于外界对氯气流量对象的干扰，还可以进一步用温度压力补偿器对其进行温度和压力补偿。The chlorine gas control loop includes a chlorine gas flow regulator, a regulating valve, and a chlorine gas flow transmitter connected in sequence; Pneumatic diaphragm valve. Preferably, a temperature and pressure compensator can be used to compensate the external interference to the chlorine gas flow object for temperature and pressure.
该丙烯混合气控制回路包括依次连接的丙烯混合气流量调节器、丙烯调节阀、丙烯流量变送器；该丙烯混合气流量调节器选用PI调节规律，该丙烯流量变送器选用漩涡流量变送器、该丙烯调节阀气动薄膜柱塞型单座调节阀。对于外界对丙烯混合气流量对象的干扰可以用Pt100热电阻变送器和电容式压力变送器对其进行温度和压力补偿。The propylene mixed gas control circuit includes a propylene mixed gas flow regulator, a propylene regulating valve, and a propylene flow transmitter connected in sequence; the propylene mixed gas flow regulator adopts PI regulation law, and the propylene flow transmitter adopts vortex flow transmission Device, the propylene regulating valve pneumatic film plunger type single-seat regulating valve. For the external interference on the flow object of propylene mixed gas, Pt100 thermal resistance transmitter and capacitive pressure transmitter can be used for temperature and pressure compensation.
该氯气控制回路和该丙烯混合气控制回路经该比值调节器连接。The chlorine gas control loop and the propylene mixed gas control loop are connected through the ratio regulator.
以上，仅为本实用新型的较佳实施例，但本实用新型的保护范围并不局限于此，任何熟悉本技术领域的技术人员在本实用新型揭露的技术范围内，可轻易想到的变化或替换，都应涵盖在本实用新型的保护范围之内。因此，本实用新型的保护范围应该以权利要求所界定的保护范围为准。The above are only preferred embodiments of the present utility model, but the scope of protection of the present utility model is not limited thereto. Any skilled person familiar with the art within the technical scope disclosed by the utility model can easily think of changes or Replacement should be covered within the protection scope of the present utility model. Therefore, the protection scope of the present utility model should be determined by the protection scope defined in the claims.
Claims (5)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010202287747U CN201762268U (en) | 2010-06-18 | 2010-06-18 | Chlorohydrination reaction control system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010202287747U CN201762268U (en) | 2010-06-18 | 2010-06-18 | Chlorohydrination reaction control system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201762268U true CN201762268U (en) | 2011-03-16 |
Family
ID=43714878
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010202287747U Expired - Fee Related CN201762268U (en) | 2010-06-18 | 2010-06-18 | Chlorohydrination reaction control system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201762268U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104607024A (en) * | 2014-12-23 | 2015-05-13 | 中国天辰工程有限公司 | Treatment method of acid-containing tail gas of chlorohydrination reaction |
-
2010
- 2010-06-18 CN CN2010202287747U patent/CN201762268U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104607024A (en) * | 2014-12-23 | 2015-05-13 | 中国天辰工程有限公司 | Treatment method of acid-containing tail gas of chlorohydrination reaction |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102512931B (en) | Method for preparing sodium hydrosulphite by utilization of tail gas from acyl chloride production | |
| JPH0362641B2 (en) | ||
| CN112546829A (en) | Double-alkali carbon dioxide cyclic absorption device and process | |
| CN201762268U (en) | Chlorohydrination reaction control system | |
| CN110255504A (en) | The system and technique of tower continuity method production sodium hypochlorite | |
| PL69878B1 (en) | ||
| CN103101883B (en) | Method for producing and activating food additive stabilized chlorine dioxide solution | |
| CN201785327U (en) | System for preparing epoxypropane by chlorhydrin method | |
| CN107033096A (en) | The synthetic method of the chlorobenzene diozaiole of 2 sulfydryl 6 | |
| US4859447A (en) | Process for the production of sodium hydrosulfite | |
| CN105293523A (en) | Continuous preparation method for production raw material ammonia water of ketazine process hydrazine hydrate | |
| CN210366984U (en) | System for tower continuous method production sodium hypochlorite | |
| US4788041A (en) | Apparatus for the production of sodium hydrosulfite | |
| CN102730771B (en) | Production of high purity sodium-free high activity composite nickel carbonate by three-step continuous process | |
| CN106444651A (en) | DCS control method of acid making process in hydrogen chloride production | |
| CN104628598A (en) | Device for industrially producing hydroxyl acetonitrile | |
| CA2104488C (en) | High yield sodium hydrosulfite generation | |
| CN105753677A (en) | Method for recovering acetone and diethylamine from mother liquor obtained after propacetamol hydrochloride ammonification | |
| RU2226295C2 (en) | Method of automatically controlling process of production of glycerol dichlorohydrines via allyl chloride hypochlorination | |
| CN205868225U (en) | Device in quick displacement reaction cauldron gaseous phase space | |
| SE452450B (en) | PROCEDURE FOR MANUFACTURING A UNDERLYCHLORIC ACID SOLUTION OF CHLORGE GAS AND DEVELOPMENT PROCEDURE | |
| CN104446795B (en) | A kind of adjustable potassium sulfate compound fertilizer ammonification production technology of reaction heat | |
| CN102319639A (en) | Preparation and addition method and addition device of sulfurous acid in copper and lead-zinc separation process | |
| CN220026122U (en) | Device for controlling temperature of anti-disproportionation reactor | |
| CN202924721U (en) | Electronic-grade hydrochloric acid industrialized preparation device system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20110316 Termination date: 20110618 |