CN2350120Y - Thermal balance high-pressure energy-saving reactor - Google Patents

Thermal balance high-pressure energy-saving reactor Download PDF

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CN2350120Y
CN2350120Y CN 98240557 CN98240557U CN2350120Y CN 2350120 Y CN2350120 Y CN 2350120Y CN 98240557 CN98240557 CN 98240557 CN 98240557 U CN98240557 U CN 98240557U CN 2350120 Y CN2350120 Y CN 2350120Y
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heat exchanger
gas
reactor
temperature
reaction
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CN 98240557
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Chinese (zh)
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楼寿林
楼韧
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杭州林达工业技术设计研究所
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The utility model relates to an energy-saving reactor for pressurization gas-solidoid catalytic reaction. After unreacted gas and reaction gas carry out heat exchange and temperature rise in a heat exchanger in a reactor tower, the temperature of the unreacted gas is raised further by external hot gas, and the unreacted gas enters a catalyst layer to react. The utility model is suitable for the case that reaction heat is insufficient to maintenance reaction self-heating to proceed, such as methanation reactor with hydrocarbon of low concentration can make use of the residual heat of the factory fluid reasonably to implement the heat balance operation of the reactor, and a normally open electric heater is not needed to compensate heat to maintain production operation, so the economic effects of electricity saving and energy saving are achieved.

Description

一种热平衡高压节能反应器 A thermal energy balance a high pressure reactor

本实用新型是一种气-固相催化反应装置,用于流体催化反应和传热过程,属化学工程领域,特别适用于低反应气成份下的甲烷化过程,也可用于其他低反应热的合成过程。 The present invention is a gas - solid-phase catalytic reaction apparatus for fluid catalytic reaction and heat transfer processes, is a chemical engineering, the process is particularly suitable for the methanation reaction at low gas component, it can also be used other low thermal reaction Synthesis.

众所周知,氢、氮气合成氨或氢、一氧化碳等气体加压下合成甲醇、甲醚和甲烷化反应都是强放热反应。 The synthesis of methanol, dimethyl ether and methanation reactions are highly exothermic gas is well known, hydrogen, nitrogen, ammonia, or hydrogen and carbon monoxide pressure. 一般工艺条件下,这类反应器设计所要着重解决的问题是及时移去反应热以防止触媒过热失活。 Under normal process conditions, such as reactor design problem to focus the heat of reaction is removed in a timely manner to prevent overheating of the catalyst deactivation. 这类反应可以利用出触媒筐高温反应气来加热进反应器的低温气体以维持反应自热进行。 Such reactions may utilize a catalyst basket into the high-temperature reaction gas to heat the low-temperature gas from the reactor to maintain the reaction autothermally. 但反应热的多少与反应气中参与反应的有效成份有关。 But how much active ingredient and reaction hot gases involved in the reaction concerned. 例如在合成氨生产中用甲烷化来精制合成氨原料气,原料气中每1%(体积比)一氧化碳与氢反应生成甲烷和水产生的反应热,在绝热下温升69℃,目前氨厂一般控制甲烷化进口气中一氧化碳气在0.6%左右,可以满足反应的自热进行。 For example, in ammonia production by methanation purified ammonia synthesis feed gas to the feed gas for each 1% (by volume) carbon monoxide and hydrogen react to form methane and water reaction heat generated, the adiabatic temperature rise at 69 deg.] C, the current general control ammonia plant methanation of carbon monoxide gas in the inlet gas is about 0.6%, to meet the autothermal reaction. 在近年来出现的中压甲醇甲烷化工艺中,甲烷化进口一氧化碳为0.3~0.6%,采用预热进塔气等方法尚能达到高压自热甲烷化反应。 In recent years pressure methanol process of methanation, the methanation of carbon monoxide inlet is 0.3 to 0.6%, preheating air into the tower or the like can still reach a high pressure autothermal methanation reaction. 但在更低一氧化碳含量下就难以自热进行,需常开电加热器来维持运行,因而导致耗电耗能。 However, it is difficult to lower the carbon monoxide content of the heat conducted from the need to maintain the normally open electric heater run, resulting in energy consumption.

本实用新型的任务是依据气-固相催化反应的热效应和传热规律解决现有技术存在的问题,寻找一种低反应热下能达到热平衡连续反应的节能反应器。 This utility is based on the new task of the gas - the thermal effect and the heat transfer solid-phase catalytic reaction of law solve the problems of the prior art, looking at a low-energy heat of reaction to reach thermal equilibrium reactor continuous reaction.

一种用于加压下气-固相催化反应的节能型反应器,具有反应器承压外筒P,触媒筐R和换热器E组成的内件,触媒筐R有盖板H,筒体S,底部花板J和内装的触媒K,调温装置C和Cb,塔内换热器有管式或板式换热器E1,或E1和E2,主要是反应器设有管b2和b3联通低温换热器和高温换热器的未反应气通道或高温戴热气通道,进外筒P的未反应气1经塔内换热器E1换热升温为未反应气2后再经高温换热器E2与外来高温戴热气进一步换热升温为未反应气3,再进触媒筐R进行反应。 An apparatus for gas under pressure - the solid phase catalytic reaction energy type reactor, a reactor having a pressure within the outer cylinder member P, the heat exchanger and the catalyst basket R E consisting of a cover plate catalyst basket R H, the cartridge body S, the bottom of the tubesheet and the enclosed catalyst J K, C and the temperature control device Cb, tower heat exchanger with a tube or plate heat exchanger E1, or E1 and E2, the main reaction tube provided with b2 and b3 Unicom unreacted unreacted gas cryogenic heat exchanger and a high temperature or a high temperature gas passage wear hot gas path, into the outer cylinder 1 through P column raised heat exchanger E1 unreacted 2 before high-temperature gas exchange E2 and the high temperature heat alien wearing heat exchanger is further warmed unreacted gas 3, R housing and then into the reaction catalyst. 上述高温换热器E2可设在外筒P内,这时高温戴热气6由管b2进入换热器E2,在低温换热器E1换热升温后的未反应气2经高温换热器E2与外来戴热气6进一步换热升温为未反应气3再进触媒筐R进行反应。 E2 the high-temperature heat exchanger may be provided within the outer tube P, this time the high-temperature wear E2 hot gas enters the heat exchanger 6 by the tube b2, the unreacted gas in the cryogenic heat exchanger E1 2 warming E2 and the high temperature heat exchanger wear alien heat exchanger 6 further warmed unreacted gas into the catalyst basket then R 3 is reacted. 高温换热器也可设在外筒P外,这时进外筒P经低温换热器E1换热升温的未反应气2由管b2引到塔外经高温换热器E2与戴热气进一步换热升温为未反应气3再进触媒筐R进行反应。 The high temperature heat exchanger may be provided outside the outer tube P, then P into the outer cylinder through the cryogenic heat exchanger E1 unreacted exchanger 2 by the heating gas introduced into the column tube b2 foreign economy and wear high temperature heat exchanger E2 further change unreacted gas temperature rises and then into the catalytic basket 3 R reaction. 反应器的工作压力为3.0~32MPa,戴热气压力为0.5~32MPa。 Working pressure in the reactor is 3.0 ~ 32MPa, wear of the hot gas pressure 0.5 ~ 32MPa. 戴热气的工作压力可低于反应器的工作压力,也可以相等,戴热气可为氨合成出塔热气。 The wearing hot working pressure below the operating pressure of the reactor, may be equal to, hot air may be worn out ammonia synthesis tower heat. 戴热气也可为变换热气。 Wear heat can also be converted heat.

下面结合附图,作进一步说明。 DRAWINGS, further description.

图1是高温换热器设在外筒外的由外筒P触媒筐R和低温换热器E1组成的反应器示意图。 Figure 1 is a schematic view of a high temperature heat exchanger disposed outside of the outer reactor tube by the outer cylinder housing the catalyst P R and the cryogenic heat exchanger E1 composition.

在图1中,在受压外筒P中,上部触媒筐R由盖板H、简体S、底部花板J和内装触媒K。 In Figure 1, the pressure P in the outer cylinder, an upper cover plate by the catalyst basket R H, simplified S, and the interior bottom tubesheet J catalyst K. 触媒层中有换热管胆Cb,盖板上有集气室D,下部换热器E1为列管式,未反应气1进入外筒在下部列管换热器E1的管间被来自触媒筐R的反应热气4加热升温为气体2,然后经管b2出塔去塔外换热器被高温戴热气加热升温为气体3,再由图1中管b3进塔到触媒层反应,出触媒层气体4在塔内换热器E1管内传热给管外气2,而冷却到温度例如100℃的气体5出塔。 Heat exchange tubes in the catalyst layer with a bile Cb, D has a plenum on the cover plate, a lower portion of the heat exchanger E1 is tubular, the unreacted gas from the catalyst is between 1 into the cylindrical outer tube at the lower portion of the column tube heat exchanger E1 R 4 basket hot reaction gas 2 is heated up, and then the column to column administered b2 external heat exchanger is heated up wearing high-temperature hot gas 3, and then into the tower by a pipe b3 to FIG. 1 the reaction catalyst layer, the catalyst layer 4 a heat transfer gas to the outer tube 2 air column in the tube heat exchanger E1, cooled to a temperature of 100 deg.] C, for example, column 5 a gas.

图2中即为这种反应器换热器的传热关系示意图。 Heat transfer is the schematic diagram of such a reactor heat exchanger 2. 在塔内低温换热器E1中未反应气被反应气加热,温度由T1升高到T2,反应气温度由T4降低到T5,然后未反应气在高温换热器中被高温戴热气例如氨合成塔出塔气或高温变换气加热由T2升温至T3,戴热气由T6降温到T7,未反应气进触媒筐,完成反应为反应气。 In column cryogenic heat exchanger E1 unreacted gas heated by the reaction gas, the temperature is increased from T1 to T2, the reaction temperature decreased from T4 to T5, and the unreacted gas is put in a high temperature heat exchanger, a high temperature hot gas such as ammonia synthesis of a column tower or a high temperature gas heated up by the gas conversion T2 to T3, T6 to wear hot gas cooled by the T7, unreacted gas into the catalyst basket, to complete the reaction of the reaction gas. 由于反应热小和存在散热,反应气温T4低于未反应气温T3。 Since the presence of heat and a smaller heat of reaction, the reaction temperature is lower than that in the reaction temperature T4 T3. 因此不可能用反应气来加热未反应气使由T2升温到T3,必须用另外的高温戴热气来加热。 Thus impossible to heat the reaction gas so that the unreacted gas was heated from T2 to T3, with additional heat must wear high-temperature heating.

图3是高温换热器E2设在高压外筒P内(由外筒P、触媒筐R和高低温换热器E1、E2组成的)反应器示意图。 3 is a schematic high-temperature heat exchanger E2 outer cylinder disposed within the high pressure P (outer cylinder P, R and catalyst basket high temperature heat exchangers E1, E2 composition) reactor. 图中上部触媒筐R由盖板H、筒体S、底部花板J和内装触媒K,触媒层中有冷气分布器C,用冷气9来调节触媒层温度,图中下部低温换热器E1和高温换热器E2均为螺旋板式换热器。 FIG catalyst in the upper housing by a cover plate R K H, the cylinder S, and the interior bottom tubesheet J catalyst, the catalyst layer has a distribution of cool air C, and 9 with the cold air to regulate the temperature of the catalyst layer, the lower part of the cryogenic heat exchanger E1 FIG. and the high temperature heat exchanger E2 are spiral heat exchangers. 未反应气1进入外筒P后进低温换热器E1的冷气通道被出触媒筐R的热反应气4加热升温为气体2,然后在高温换热器E2的冷气通道中被由管b3引入的高温戴热气6进一步加热,升温到气体3去触媒筐反应,戴热气降温为气体7由管b2出塔,出触媒筐R的反应气4在低温换热器E1热气通道传热给未反应气后降温为气体5后经管b1出塔,下端b4中气体8为调节反应器触媒温度用。 Unreacted gas enters the outer cylinder 1 backward P cryogenic heat exchanger cool air passage E1 is a thermal reaction catalyst basket R 4 gas heating ramp 2 gas is then introduced into a tube in a high temperature heat exchanger b3 cool air passage E2 in Dai 6 further heated hot gas temperature, the gas temperature was raised to 3 to the reaction catalyst basket Dai hot cooling gas 7 from the pipe column b2 out, out of the reaction gas to the catalyst basket R 4 is a low temperature heat exchanger E1 unreacted gas hot gas path after cooling gas out of the column 5 administered b1, b4 of the lower end of the gas regulator 8 as reactor temperature with a catalyst.

实施例,年产10万吨合成氨装置采用等高压甲醇甲烷化装置。 Example, 100,000 tons of ammonia plant using high-pressure methanol methanation like. 精炼合成氨原料气代替铜洗法除微量CO,高压甲烷化塔采用图3型式,直径用φ1000,内装镍基甲烷化触媒5M3,入塔气量40000 NM3/h,进甲烷化塔CO 0.05%,CO20.001%,CH40.5%,H274.589%,N224.86%,气温80℃,进甲烷化塔低温换热器E1后升温到270℃,再在高温换热器E2中与经管b3引入,由合成氨出塔热气6气温360℃戴热气换热,后者降温到300℃的气体7经管b2出塔,未反应气升温到330℃进触媒筐反应,出触媒筐气温310℃,与在E1中与入塔气换热后降温到120℃出塔。 Refinery ammonia synthesis feed gas instead of copper in addition to trace CO.'s washing method, a high-pressure type methanation column employed in FIG. 3, with a diameter φ1000, a nickel-based methanation catalyst 5M3 interior, the gas column 40000 NM3 / h, into the methanation column CO 0.05%, CO20 .001%, CH40.5%, H274.589%, N224.86%, temperature 80 ℃, into the methanation column cryogenic heat exchanger E1 was heated to 270 ℃, and reintroduced into the high-temperature heat exchanger b3 administered E2, from the ammonia column 6 steam temperature heat exchanger 360 ℃ wear, which is cooled to 300 deg.] C of the gas out of the column 7 administered b2, unreacted feed gas was raised to 330. the reaction catalyst basket deg.] C, a temperature of 310 deg.] C catalyst basket, and in E1 into the tower with the air heat exchanger to cool 120 ℃ the column.

本实用新型合理地利用工厂富有的工艺气余热实现反应器的热平衡运行,不需要常用电加热器来补偿热量维持生产运行,达到了省电节能的经济效果。 The present invention rational use of the plant rich process gas heat to achieve the thermal balance of the reactor operation, the electric heater does not need to compensate for the heat used to maintain the production run to achieve the economic effect of energy saving.

Claims (8)

  1. 1. 1. 一种用于加压下气-固相催化反应的节能型反应器,具有反应器承压外筒P,触媒筐R和换热器E组成的内件,触媒筐R有盖板H,筒体S,底部花板J和内装的触媒K,调温装置C和Cb,塔内换热器有管式或板式换热器E1,或E1和E2,其特征是反应器设有管b2和b3联通低温换热器和高温换热器的未反应气通道或高温戴热气通道,进外筒P的未反应气1经塔内低温换热器E1换热升温为未反应气2后再经高温换热器E2与外来高温戴热气进一步换热升温为未反应气3,再进触媒筐R进行反应。 An apparatus for gas under pressure - the solid phase catalytic reaction energy type reactor, a reactor having a pressure within the outer cylinder member P, the heat exchanger and the catalyst basket R E consisting of a cover plate catalyst basket R H, the cartridge body S, the bottom of the tubesheet and the enclosed catalyst J K, C and the temperature control device Cb, tower heat exchanger with a tube or plate heat exchanger E1, or E1 and E2, wherein the reactor tube is provided and b2 b3 unreacted unreacted gas Unicom cryogenic heat exchanger and a high temperature or a high temperature gas passage wear hot gas path, into the outer cylinder 1 through P column cryogenic heat exchanger E1 warmed unreacted gas after over 2 high-temperature heat exchanger E2 and exotic high temperature wear further heat exchanger heated unreacted gas 3, R housing and then into the reaction catalyst.
  2. 2. 2. 根据权利要求1所述的节能型反应器,其特征是高温换热器E2设在外筒P内,高温戴热气6由管b2进入换热器E2,在低温换热器E1换热升温后的未反应气2经高温换热器E2与外来戴热气6进一步换热升温为未反应气3再进触媒筐R进行反应。 Energy according to claim 1 of the reactor, characterized in that the high-temperature heat exchanger P E2 disposed within the outer cylinder, the hot gas temperature wear a tube 6 b2 enters the heat exchanger E2, E1 in the low temperature heat exchanger warming 2 unreacted gas unreacted gas into the catalyst 3 and then through the high temperature heat exchanger housing R E2 and foreign Dai 6 further heat exchanger for the heating reaction.
  3. 3. 3. 根据权利要求1所述的节能型反应器,其特征是高温换热器设在塔外,进外筒P经低温换热器E1换热升温的未反应气2由管b2引到塔外经高温换热器E2与戴热气进一步换热升温为未反应气3再由管b3进触媒筐R进行反应。 Energy according to claim 1 of the reactor, characterized in that the high-temperature heat exchanger disposed in the outer column, the outer tube P into the cryogenic heat exchanger by unreacted exchanger E1 by the temperature rise of the gas pipe 2 to the column lead foreign economic b2 the high temperature heat exchanger to further heat exchanger E2 and wear unreacted gas is heated further by the reaction tube 3 into the catalyst basket b3 R.
  4. 4. 4. 根据权利要求1所述的节能型反应器,其特征是反应器的工作压力为3.0~32MPa。 Energy according to claim 1 of the reactor, wherein the reactor operating pressure is 3.0 ~ 32MPa.
  5. 5. 5. 根据权利要求1所述的节能型反应器,其特征是戴热气压力为0.5~32MPa。 Energy according to claim 1 of the reactor, characterized in that the wearing pressure of the hot gas is 0.5 ~ 32MPa.
  6. 6. 6. 根据权利要求1所述的节能型反应器,其特征是戴热气为氨合成出塔热气。 Energy according to claim 1 of the reactor, wherein the wear heat of the ammonia synthesis tower heat.
  7. 7. 7. 根据权利要求1所述的节能型反应器,其特征是戴热气为变换热气。 Energy according to claim 1 of the reactor, wherein the wear hot transform heat.
  8. 8. 8. 根据权利要求1所述的节能型反应器,其特征是戴热气的压力低于反应器的工作压力。 Energy according to claim 1 of the reactor, wherein the wear is lower than the pressure of the hot gas of the reactor operating pressure.
CN 98240557 1998-09-14 1998-09-14 Thermal balance high-pressure energy-saving reactor CN2350120Y (en)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN100386138C (en) 2003-12-06 2008-05-07 杭州林达化工科技有限公司 Process and equipment for internal heat exchanging catalytic reaction
CN101966440A (en) * 2010-10-19 2011-02-09 西北大学 Cambered plate type gas-solid phase reactor

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN100386138C (en) 2003-12-06 2008-05-07 杭州林达化工科技有限公司 Process and equipment for internal heat exchanging catalytic reaction
CN101966440A (en) * 2010-10-19 2011-02-09 西北大学 Cambered plate type gas-solid phase reactor
CN101966440B (en) 2010-10-19 2012-11-07 西北大学 Cambered plate type gas-solid phase reactor

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