CN86103332A - 改进非均相催化合成反应器以降低能量消耗的系统及其相应的反应器 - Google Patents
改进非均相催化合成反应器以降低能量消耗的系统及其相应的反应器 Download PDFInfo
- Publication number
- CN86103332A CN86103332A CN86103332.9A CN86103332A CN86103332A CN 86103332 A CN86103332 A CN 86103332A CN 86103332 A CN86103332 A CN 86103332A CN 86103332 A CN86103332 A CN 86103332A
- Authority
- CN
- China
- Prior art keywords
- flow
- reactor
- catalyst bed
- diameter
- catalyst
- 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 - Lifetime
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/04—Preparation of ammonia by synthesis in the gas phase
- C01C1/0405—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst
- C01C1/0417—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst characterised by the synthesis reactor, e.g. arrangement of catalyst beds and heat exchangers in the reactor
- C01C1/0423—Cold wall reactors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0403—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal
- B01J8/0407—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more cylindrical annular shaped beds
- B01J8/0415—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more cylindrical annular shaped beds the beds being superimposed one above the other
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0403—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal
- B01J8/0423—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more otherwise shaped beds
- B01J8/0426—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more otherwise shaped beds the beds being superimposed one above the other
- B01J8/0434—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more otherwise shaped beds the beds being superimposed one above the other in combination with two or more cylindrical annular shaped beds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
- B01J8/0449—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds
- B01J8/0453—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds the beds being superimposed one above the other
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
- B01J8/0461—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical annular shaped beds
- B01J8/0469—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical annular shaped beds the beds being superimposed one above the other
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0496—Heating or cooling the reactor
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/152—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00194—Tubes
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
- Y10T29/00—Metal working
- Y10T29/49—Method of mechanical manufacture
- Y10T29/49826—Assembling or joining
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Fluid Mechanics (AREA)
- Analytical Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
改进非均相合成特别是氨和甲醇合成反应器以降低能耗的系统。本方法是在反应器的至少部分触媒床(气体在其中是轴向流动的)中加进两个多孔筒壁,以便将床层径向限制起来。上述两个筒壁中至少一个上部有一个占小部分的不开孔区,并且两筒底部用一隔板封住。这样床层中的气流就基本上径向(内向外或外向内)流动了。在本发明一个具体方案中,在至少一个床的顶部采用了部分开孔或全封闭的调节板和/或有尺寸梯度的触媒层。
Description
本发明是一种增加非均相合成反应器特别是氨合成反应器转化收率并减少其能量消耗的系统。合成反应器由外壳(P)(通常是整体),内件(C)组成。内件C的外径是(D),其内装有一层或多层触媒颗粒。触媒床(K)高(Hi),位于外筒壁、内筒壁和多孔底(F)之间。外筒壁由内件的一部分构成,其内径为(Di)高度为Hi。内筒壁由输送新鲜合成气的中心输气管(T)的一部分构成,其直径De较(Di)小,高度也是(Hi)。每个触媒床的上部都是敞开的。合成气进气作轴向流动。
正如所知,在加压下进行催化合成的反应器,特别是氨、甲醇以及高级醇类的合成反应器通常由外壳(一般是整体的)和内件组成。内件中装有一层或多层不同型式具有不同特性的触媒颗粒称为触媒床。
对于放热反应,为了使得各触媒床层保持最佳温度,通常在触媒床之间对流经触媒床的气流进行冷却。冷却方式可以是在床层之间注入新鲜反应气(冷激式)即采取与进口冷气直接换热的方式。
近年来,有人提出采用气体在触媒床中作径向流动(Lummus,Topsoe,Kellogg,美国专利3918918和4181701号,欧洲专利申请007743-A1号)或轴向-径向混流型(Ammonia Casale美国专利4372920和4405562号)的反应器。这些反应器和原先的轴流式反应器相比进了一步。尤其是在触媒量很大的情况下,它仍能保持较小的流经触媒床层的压力降因而可以节约能量。
气体轴向流动型要求将反应器制成矮胖型(即长径比小)。其设备费用和能耗都比较高。
Ammonia Casale专利(美国专利4372920和4405562号)大幅度地简化了合成反应器内件的结构,便于对内件进行检修和装卸触媒,同时也降低了气体的压力降。
在上述几个专利中,每层触媒床实际上都是由多孔外壁、多孔内壁和一个封底组成,触媒床上部是完全敞开的。在上述内外两个筒壁中至少有一个筒壁上部不开孔。筒壁的不开孔区和位于上述两个筒壁上端的敞开截面形成一个区域,使得流经触媒的小部分气体仍其本上是沿轴向流动而大部分气体则是沿径向流经位于筒壁开孔区的大部分触媒床。上述筒壁上端,其平面与前述筒壁的轴线相垂直。
因此,基本上沿轴向流动所占的气体量是完全由筒壁上部至少有一个筒壁不开孔区的高度所确定。而不开孔区只占整个筒壁高度的较小部分。
长径比大于10(即径长比小于0.1)的反应器最好按照上述技术进行设计。
在当今世界经济状况下,对现有大多数采用轴流式反应器(如氨合成反应器等)的装置进行现代化改造具有重要意义。这些轴流式合成反应器的特点是长径比小,之所以这样是因为上面所说的原因,即要保持较低的压力降。轴流式反应器不但能耗高而且还有其它的缺点,特别是那种“lozenge”式反应器,因为只有一个单层高触媒床,因而压力降很大导致能耗高,而且底部触媒由于受压迫,容易损坏,丧失部分活性。
本发明的目的是为在加压下进行非均相催化合成的反应器提供一个降低能量消耗的方法,特别适合于对那些常用的低长径比轴流式反应器,如Kellogg,ICI型反应器进行技术改造。上述这些反应器为七十年代后期建造的大型(日产800~1500吨)装置所广泛采用。上述大型工厂的特点,除了产量大之外,就是将装置自产的蒸汽送进一定的循环系统以带动透平压缩机和采用上面提到的低效率轴流式合成反应器。
上述装置能量消耗高的特点在能源可以廉价获得的年代中并不成为一个关键的因素。而造成能量消耗高的原因之一是因为这些装置采用轴流式反应器。
按照本发明,就不难对那些高能耗的轴流式反应器,特别是那些低长径比的反应器进行改造并取得很大的好处。这只要通过更改触媒筐结构使得至少在一部分触媒层中的气流流向由轴向变为以径向为主,最好轴向流动和径向流动并存或者完全径向(可以由外向内也可由内向外)就行。
因而,正如导言和主权利要求中所描述,本发明的方法是以下列改造触媒床形状的步骤和手段为特点的:
(a)在内件C外壁之内并靠近该内件外壁处加进一个圆筒,该圆筒高为Hi,直径为D′i。D′i应稍小于Di,Di是内件C的内直径。所加圆筒在高度Hi上的大部分区域开孔;
(b)再加一个内圆筒。内圆筒上在触媒床高度Hi上的大部分区域也开孔。内圆筒直径比前面说到达的中心输气管T的直径De略大;
(c)在触媒床底部F安装一个外径为Di内径为D′e的环形封底。
按照本发明的一种实施方案,在上述两个被加进的筒壁当中至少有一个筒壁(Fe和/或Fi)上有一不开孔区域(不开孔区域高度为Hi-H′i,占Hi的一小部分),从而使得合成气在催化剂床层中以径向流动为主(轴向-径向流),其流向可以是由外向内,也可以是由内向外。
最好,把流经按上述实施方案改造过的触媒层上部敞开截面的气流分成两股。其大股气流径向流经至少一个筒壁(Fe和/或Fi)的开孔区H′i,而小股气流则轴向流经未开孔的区域(Hi-H′i)。
本实施方案与上面说过的Ammonia Casale专利的区别之一是:按本方案,以轴向流动为主的那股气流所占的比例一般比较高(甚至筒壁沿高度方向可以大部分不开孔)而剩下的那股气流即径向流经筒壁开孔区的气流比例要来得小一些。
上述本发明实施方案的一种型式是:在内筒壁上部保留较小的不开孔区域,并使合成气流经触媒床汇集在由直径为De的输气管T的和高度为H′i的部分内筒壁Fi(直径D′e)所包围的环形空间内。
在本方案的第二种型式中,外筒壁上有一较小的不开孔区域。而其开孔区域与反应器内件的内壁形成反应气的流道。
如果内件中各床层高度不同即各层触媒的高度与直径的比例不同的话,上述轴向气流和径向气流之间的比例可以随着床层高度变化而改变。例如在应用本发明改造Kellogg型合成反应器时,就遇到Kellogg型反应器中床层高度递增的情况。
本发明的一个优点在于:可以通过安装触媒层上部调节板减少通过某些触媒层上部的轴向流动的气流甚至可以完全封死而不再有轴向气流。调节板通过减少位于加进的那两个筒壁上端之间的流通截面达到上述目的,板上开有合适的孔道(如圆孔,开槽等),也可以是全封闭的,调节板与触媒床的上表面直接接触,其开孔可以沿半径方向按一定规律分布如开孔面积由内向外增加(对于气流由内向外流动者,也可反过来,由内向外减少)。
本发明的另一个特点是:可以借助触媒的粒度大小不同以实现轴向气流的减少。例如触媒床上部由小颗粒触媒组成,而底下在气流方向为径向的区域内充填大颗粒触媒。而且所说的触媒层厚度由内向外递减(当气流方向是由内向外流动时)或递增(当气流方向是由外向内流动时)。
本发明的又一个特点是上述调节板可以是完全封闭的并座落在床层上端。
通过对附图中所示的几个比较好但非限制性实施例的说明可以充分了解本发明。附图分别画出几种原先的反应器和按本发明改造后的反应器一部分的纵剖面示意图。图1A为已有的Kellogg反应器,图1B为已有的ICI反应器,图2A,2B,3A,3B及图4、5、6为按本发明改造后的反应器。更具体地说,图2A及2B表示按本发明的方法将图1A及1B所示一般轴流式反应器改造成为由外向内的径向流动为主的反应器的情况而图3A及3B则表示改造成由内向外的径向流动的情况,图4是在图2A改造(由外向内流动)的基础上,在上两个触媒床上增加调节板。图5则表示按本发明的方法对大长径比(如≈10)的反应器,如TVA(Tennessee Valley Authority)一类反应器所进行的改造方案。而图6是在图2A由外向内流动的径向反应器的下面两个床层上加上封闭隔板的情形。
图1表示具有四层触媒床(Ⅰ至Ⅳ)的常用的Kellogg型反应器,合成气FG在四个床层中均匀轴向流动(箭头A的方向),共有四个急冷气喷头1-4,每个床层上各有一个。图1B表示所谓“ICI型”的反应器,它只有一层触媒,不过被两个菱形(lozenge)急冷喷头L1及L2分成三段Ⅰ,Ⅱ,Ⅲ。在所有的图中,都注有英文字母和阿拉伯数字,所代表的含意如下:P:受压外壳;C:内件;E:外壳P内壁和内件C外壁之间的气体通道,通常使冷反应气FG流经该通道以冷却外壳表面;K:指通常的触媒,对于图1触媒分成在四个触媒筐Ⅰ~Ⅳ中,对于图2,在Ⅰ~Ⅲ中,每个触媒筐有一定的高度如图1中为H1,H2,H3,H4,筐的外径都是Di,约等于内件C之内径,触媒筐的内径De约为中心输气管T的外径;S:间接热交换器;6:反应过的气体出口。
在通常的轴流式反应器,例如图1A所示的Kellogg型反应器中,新鲜反应气FG由反应器底部进入,向上流经外壳P与内件C之间的通道E到上部气-气热交换器S的管外(管内为热的反应气RG)而后通过环形通道S′向下返回并与急冷气1混合进入第一层触媒床Ⅰ(流向为A)。在触媒中气流方向完全是轴向的。接着轴向流动的气体由第一层触媒床Ⅰ底部流出并与急冷气2混合进入并轴向流经触媒床Ⅱ,在触媒床Ⅱ底部与急冷气体3相混合,该急冷的气体进入并轴向通过触媒床Ⅲ,并与急冷气体4相混合,轴向通过触媒床Ⅳ,热的反应过的气体5,汇集在触媒床Ⅳ的底部,并进入中心输气管T流动至顶部热交换器与新鲜气FG′进行换热,然后经由反应器出口6离开反应器。
图1B表示另一种常用的完全轴向流动的反应器。它和图1A所示反应器的不同在于:急冷气体Q1与Q2由反应器顶部分别经过Q′1与Q′2到菱形喷头(“lozenge”)L1与L2,通过L1与L2进入触媒层Ⅰ,Ⅱ及Ⅲ之间(这种“lozenge”式反应器亦称ICI“lozenge”反应器)。新鲜气FG反应器顶部进入,在气体通道E中向下流动成为进入底部热交换器S的气体FG′,并经由中心输气管T向上返回。气体在输气管T出口处向下折,成为流经触媒层的轴向气流A。反应过的气体RG由触媒层Ⅲ底部汇集成出口气6。由于技术人员对这种为大家所熟知的反应器是很熟悉的,所以在此不再详细叙述了。一般的说,这种常用的反应器压力降很大因而消耗大量的能量而且它们所用的触媒K是低效大颗粒型(6~16毫米)的。各触媒床层的高度一般由上至下递增即在图1A中H1<H2<H3<H4。
按本发明对触媒筐Ⅰ,Ⅱ,Ⅲ,Ⅳ的内件进行改造从而基本实现径向流动同时可以采用效率比较高的小颗粒触媒(1.5~3毫米)并且可以保持较小的压力降。这样就消除了上面说到的那些反应器的缺点,也消除了一些其它的不足之处。
新的系统如图2A和图2B所示。根据本发明的主要特点,原来的轴向流动(在本例中,所有的触媒床都是轴向流动的)改换为基本上径向流动,最好是小股气流轴向流动和大股气流径向流动。为此,每个触媒筐Ⅰ、Ⅱ、Ⅲ、Ⅳ都由直径(D′e)比输气管T的直径(De)大的基本上开孔的内壁Fi和直径(D′i)比内件C内径(Di)小的基本上开孔是外壁(Fe)所包围。每个触媒筐底部均有未开孔封底FO。图2A表示第一种实施方案,其外壁Fe在触媒筐的全高Hi上都开孔且具有相同直径D′i相反,内壁Fi只在部分高度H′i上开孔,而在剩下的部分Hi-H′i不开孔。内壁Fi的直径在H′i的高度上是D′e,在Hi-H′i高度上缩小至输气管T的直径De,借以实现上述部分开孔的目的。因而,经过预热的气体FG′在各触媒床Ⅰ、Ⅱ、Ⅲ、Ⅳ中都是小部分沿轴向流经未开孔高度Hi-H′i(在该区域内壁(Fi)实际上与输气管T相接触)而大部分则在开孔区域Hi作径向流动。换言之,反应气分为两股,小股A轴向流动,大股B径向流动。在图2A与2B中,径向流动是由外向内,也就是新鲜气进入外壁Fe(直径D′i)和内件C(直径为Di较D′i稍大)之间的通道,同时由于封底FO将D′e-Di所组成的环形截面都封死,气流由外向内流动并汇集于内壁开孔部位H′i(直径为D′e)与输气管T(其直径De稍小于D′e)之间的空间。这一由De-D′e所组成的环形空间是敞开的,轴向流动和径向流动的气体都经由这一空间流出。由触媒筐Ⅰ出来的气体与急冷气体2混合后又经过触媒筐Ⅱ,也是部分轴向流动和部分径向流动的。同样地还经过触媒筐Ⅲ和Ⅳ。由最后一个触媒筐出来的反应过的气体5进入输气管T,向上流动并由反应器出口6排出,(图2A Kellogg型反应器)。
在图2B中,和上面相同的步骤也适于ICI型反应器。其不同之处为新鲜合成气FG与急冷气Q1-Q2由反应器顶部进入,而热交换器S及出口则安排在底部。除了这些次要的不同之外,按本发明方法的步骤与图2A所示的反应器是一样的:每个触媒筐都由开孔内壁Fi与外壁Fe及封闭的底FO组成。外壁Fe在整个高度上直径都是D′i且全部开孔,而内壁Fi在H′i高度上的开孔区域直径为D′e,而在不开孔的Hi-H′i上直径与输气管T的直径De相同。因而占小部分的触媒筐的上部(高为Hi-H′i,内直径为De)是不开孔的,只有小部分轴向流动的气流通过。而流经占大部分的具有Hi高度的触媒筐开孔区域(具有D′i-De的环形宽度)的是占大部分的径向气流,由外向内流动。内件内壁(直径Di)和触媒筐开孔外壁Fe之间的敞开通道构成由外向内径向未反应气体的通道(流向B)。而直径为D′e的内壁Fi与直径为De的输气管之间的较短的通道CO成为反应过的气体RG的收集器。这些反应过的气体是由外向内沿径向流过触媒筐上H′i的高度。由最后一个触媒筐Ⅲ底部出来的反应过的气体RG流经热交换器后由6出去。
在图3A与3B中表示了由内向外流动的实例。在这些实例中,内壁Fi在全高度Hi上开孔具有不变的直径D′e(D′e较输气管T的直径De稍大)。而外壁Fe只在H′i高度上开孔,在Hi-H′i高度上不开孔,在H′i上的直径是D′i,在Hi-H′i高度上与内件直径Di相同。底部不开孔环形封底由输气管直径De处延伸至开孔外壁Fe直径D′i处。在图2A及图2B中该封底FO在内件C的内表面处封接,而在图3A及图3B中的由内向外流动的反应器中,封底则在输气管T的外表面处封接。在图3A中上述封底FO与输气管T之间的环形密封用SAi表示。与图2A情况相似,新鲜气FG由底部进入,由通道E向上流至热交换器S的管外。而后气流轴向冲击触媒床Ⅰ的上表面Al并在Hi-H′i区域(图中以SPO标志)沿轴向流动(流向A)。新鲜气FG也进入管T与壁Fi之间的通道并沿径向向外流(流向B),经过每个触媒筐的占大部分的下面部分H′i。反应过的气体(流向CO)汇集在内件内壁与部分开孔壁Fe之间的敞开空间。该气流CO又轴向冲击下一个触媒筐并在其较短的部分SPO轴向流动。在较长的部分H′i由内向外沿径向流动。反应过的气体汇集在反应器底部并经6流出反应器。在图3A中,热交换器S和出口6都在反应器顶部。而在图3B中,热交换器和出口6都在反应器底部。
图4表示在图2A的实施方案中,在触媒床Ⅰ与Ⅱ顶部敞开表面上加上流量调节板U。在一般的情况下,轴向流量/径向流量比例只与未开孔高度Hi-H′i与开孔高度H′i的比例有关。但在本情况下,调节板也对上面两个触媒筐中的轴向流量(Al)进行调节。最好,轴向流量调节板上的孔有不同的大小和形状,例如孔的直径由板中心向外沿半径方向增加(或减少)。该调节板可以直接放置在触媒之上。尽管各床层的高度H1,H2,H3,H4不一样但其轴向流量与径向流量的比例可保持大致一样,具体比例最好在0.02~0.2之间。还可以采用触媒尺寸不同的方法来代替调节板或者两种方法并用。触媒尺寸不同可以通过下述方法来实现:例如上层采用颗粒比下层小得多的触媒,每个触媒层的厚度由内向外沿半径方向减少(或相反)。还有一种方案,在某些床层不采用带孔的降压调节板而采用非开孔隔板。
图6表示一种特殊的方案。在这一方案中至少有一个触媒床,例如在本图中是Ⅰ与Ⅱ两个触媒床没有改动,与图1A所示的完全轴向流动的情况一样。同时至少有一个触媒床如图中的Ⅲ床改为轴向-径向混流并附有部分开孔的调节板U(如图4所示一样),并且至少有一个触媒床,如图中的Ⅳ床改为全径向流式的并附有全封闭隔板U′。在Ⅳ中内外两壁F′e及F′i都沿全部高度Hi开孔,而在Ⅲ中Fe是沿全高度Hi开孔的Fi只在H′i高度上开孔。未改进轴流床Ⅰ(也可能)与床Ⅱ在反应器顶部,即高度H1与H2(见图1A)不大,因而所造成的压力降也不大。
最后,图5表明:尽管本发明对于长径比(H/O)小于10的反应器特别有利,它一样能用于长径比大于10的反应器。图5所示反应器为-TVA(Temessee Valley Authorty)反应器。对于这种反应器,我们不需多加解释。
下列诸例说明本发明之优点:
例1(对比)
如图1所示具有四个绝热触媒层,3个中间急冷喷头的Kellogg反应器所达到的典型性能如下:
产量:1090公吨NH3/日
反应器入口压力:155巴(绝)
反应器出口流量:28378千摩尔/时
(包括急冷气)
反应器入口NH3含量:2%摩尔
反应器出口NH3含量:12.58%摩尔
反应器压力降△P 3.8巴
其它特性:
急冷气体温度 138.0℃
一床后急冷气流量 4347.46Kmol/h
二床后急冷气流量 4474.25Kmol/h
三床后急冷气流量 3250.35Kmol/h
压力 143.8巴(绝)
例2
按本发明进行改造过的反应器(图2A,3A及4)可达到的性能。
对反应器内件进行改造成具有四个小颗粒(1.5~3毫米)触媒床和三个中间急冷并实现轴向-径向流动的反应。
其性能如下:
产量:1090公吨NH3/日
反应器入口压力:155巴(绝)
反应器出口流量:22378 Kmol/h
(包括急冷气体在内)
反应器入口NH3含量:2%mol
反应器出口NH3含量:15.8%mol
反应器压力降△P:1.8巴
其它特性:
急冷气体温度 138.0℃
一床后急冷气流量:3277.41Kmol/h
二床后急冷气流量:3296.83Kmol/h
三床后急冷气流量:2635.83Kmol/h
压力:143.8巴(绝)
例3(对比)
如图1B所示的具有三个绝热触媒床和2个中间急冷的ICI反应器所达到的典型性能如下:
产量:1200公吨NH3/日
反应器入口压力:238巴(绝)
反应器入口流量(包括急冷
气体):28434Kmol/h
反应器入口NH3含量:3%mol
反应器出口NH3含量:14.82%mol
反应器压力降△P:10巴
急冷气体温度:150℃
例4
按本发明对例3之反应器进行改造后(图2B及3B)的性能。
反应器内件改造后具三层小颗粒(1.5~3毫米)触媒和三个中间急冷并实现轴向-径向流动。
其性能如下:
产量:1200公吨NH3/日
反应器入口压力:238巴(绝)
反应器入口流量(包括急冷
气体):22884千摩尔/小时
反应器入口NH3含量:3%摩尔
反应器出口NH3含量:18.16%摩尔
反应器压力降△P:2巴
Claims (10)
1、使非均相合成,特别是氨和甲醇合成的反应器增加转化收率和减少能量消耗的系统,该系统由外壳P和内件C组成,外壳P通常是整体的,内件的外径为D,内有分装在一层或多层触媒床K中的粒状触媒,触媒床高为Hi,位于外筒壁、内筒壁和底F之间,外筒壁是内件C的一部分并且有内径Di和高度Hi,内筒壁是输送新鲜合成气的管子T的一部分,直径为De(较Di为小),触媒筐的上截面敞开,合成气作轴向流动,本系统的特点在于至少在一个触媒床上按下述办法对触媒进行限位:
(a)在内件C外壁之内并靠近该壁处加进一圆筒,其上沿高度Hi的大部分区域开孔,圆筒壁的直径D′i略小于上述内件C的内径Di,
(b)加进一个沿其高度Hi大部分区域开孔的内筒壁,其直径为D′e比内输气管T的直径De略大,
(c)触媒床底部F安一环形封底FO,
在上述两个加进的圆筒壁(Fe及/或Fi)中至少有一个上面至少有占小部分的不开孔区Hi-H′i,这样以来触媒床中的合成气以径向流动为主(由外向内或由内向外)。
2、根据权利要求1的系统,其特征为合成气流分为通过上述加进的筒壁上开孔高度H′i(占总高度的大部分)的径向流B和通过至少一个筒壁上的上部不开孔高度(占总高度较小部分)的轴向流A。
3、根据权利要求1的系统,其特征为该上部占较小部分的不开孔区是在内筒Fi之上而且流经触媒床的合成气汇集于由直径为De的输气管T与高度为H′i(<Hi)和直径为D′e(>De)的内壁Fi的一部分组成的环形空间。
4、根据权利要求1的系统,其特征为该上部占较小部分的不开孔区是在外筒壁Fe上,外筒壁Fe的占大部分的开孔区Hi与内件C的内壁形成一通道以便反应过的气体流通。
5、根据权利要求1的系统,其特征为占大部分的开孔区的高度H′i是根据各触媒床高度Hi加以调整的,以便在每一触媒床中都得到最佳轴向流量/径向流量比。
6、根据权利要求5的系统,其特征为至少在一部分改造过的触媒床中轴向气流与径向气流的比例同时也用采用一个板来减少触媒床顶部自由截面的方法来调节。
7、根据权利要求6的系统,其特征为上述板带有孔,该孔最好具有沿着径向由内向外增加的截面积(对于由内向外流式则相反)该板置于触媒床上表面,各触媒床的轴向流量与径向流量的比例控制在0.02~0.2的范围内。
8、根据权利要求6的系统其特征为在采用调节板的同时还在触媒床层的上部采用下述方法或者用下述方法代替该为达到减少触媒床自由截面目的的调节板上层触媒颗粒比下层触媒颗粒小得多,床层厚度由内向外减少(或者气体由内向外流动时增加)。
9、根据前述权利要求的系统,其特征为至少在一部分改造过的触媒床上采用全封闭(不带孔)的板而不采用带孔的调节板以使轴向气流量为零。
10、非均相合成特别是氨反应器,其长径比(H/D)小于10,触媒床安排在增加的筒壁Fi与Fe之间,合成气流在床层的小部区域中作轴向流动,而在大部区域中作径向流动。
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CH2100/85-0 | 1985-05-15 | ||
CH210085 | 1985-05-15 | ||
CH03-238/85-0 | 1985-07-25 | ||
CH3238/85A CH666197A5 (it) | 1985-07-25 | 1985-07-25 | Reattore per aumentare la resa di conversione e ridurre i consumi energetici nelle sintesi eterogenee dell'ammoniaca. |
Publications (2)
Publication Number | Publication Date |
---|---|
CN86103332A true CN86103332A (zh) | 1986-12-31 |
CN1004611B CN1004611B (zh) | 1989-06-28 |
Family
ID=25689517
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
CN86103332.9A Expired CN1004611B (zh) | 1985-05-15 | 1986-05-14 | 改进非均相催化合成反应器以降低能量消耗的系统及其相应的反应器 |
Country Status (8)
Country | Link |
---|---|
US (3) | US4755362A (zh) |
EP (1) | EP0202454B2 (zh) |
CN (1) | CN1004611B (zh) |
CA (1) | CA1277123C (zh) |
DE (1) | DE3686783T3 (zh) |
ES (1) | ES8703812A1 (zh) |
IN (1) | IN165082B (zh) |
UA (1) | UA32508C2 (zh) |
Families Citing this family (38)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0265654A1 (en) * | 1986-09-25 | 1988-05-04 | Ammonia Casale S.A. | System and device to make catalytic basket walls for heterogeneous synthesis reactors |
IN170330B (zh) * | 1986-10-22 | 1992-03-14 | Ammonia Casale Sa | |
DE3783220T2 (de) * | 1986-11-03 | 1993-04-29 | Ammonia Casale Sa | Verfahren zur reduktion des energiebedarfs in mehreinheitenreaktoren fuer die heterogene synthese und verwandte reaktoren. |
EP0293546A3 (en) * | 1987-02-11 | 1989-06-07 | Ammonia Casale S.A. | System to deal with the efficiency of reactors for exothermic ammonia synthesis |
DE3880877T2 (de) * | 1987-02-26 | 1993-09-23 | Ammonia Casale Sa | System zur verbesserung der reaktorausbeute fuer exotherme synthese, insbesondere fuer die ammoniakreaktion. |
DE3710004A1 (de) * | 1987-03-26 | 1988-10-06 | Uhde Gmbh | Vorrichtung zur katalytischen behandlung von stickstoff und wasserstoff |
CN88103614A (zh) * | 1987-05-14 | 1988-12-14 | 阿莫尼·卡萨尔公司 | 多相合成反应器的改进 |
DE68901115D1 (de) * | 1988-06-27 | 1992-05-07 | Ammonia Casale Sa | Verfahren und reaktor fuer die exotherme heterogene synthese mit hilfe verschiedener katalytischer betten und mit externer rueckgewinnung der reaktionswaerme. |
EP0359952A3 (en) * | 1988-08-05 | 1990-07-18 | Ammonia Casale S.A. | System for the improvement of reactors for the synthesis of methanol and reactors obtained therefrom |
US5184386A (en) * | 1988-12-09 | 1993-02-09 | Ammonia Casale S.A. | Method for retrofitting carbon monoxide conversion reactors |
EP0372453B1 (en) * | 1988-12-09 | 1995-11-15 | Ammonia Casale S.A. | Method for retrofitting in situ an axial flow carbon monoxide conversion reactor. |
DE68900388D1 (de) * | 1988-12-09 | 1991-12-05 | Ammonia Casale Sa | Reaktor fuer die exotherme heterogene katalytische synthese. |
DE68906006T2 (de) * | 1988-12-21 | 1993-08-12 | Ammonia Casale Sa | Reaktoren fuer heterogene synthesen. |
CH678286A5 (zh) * | 1989-03-09 | 1991-08-30 | Ammonia Casale Sa | |
EP0386692A3 (en) * | 1989-03-09 | 1991-01-09 | Ammonia Casale S.A. | System for modifying in situ reactors for the synthesis of ammonia |
US5250270A (en) * | 1992-07-17 | 1993-10-05 | The M. W. Kellogg Company | Catalytic reactor bed |
DE4228147A1 (de) * | 1992-08-25 | 1994-03-03 | Solvay Fluor & Derivate | Verfahren und Vorrichtung zur Herstellung von Diglycerin |
DE69426517D1 (de) * | 1993-10-29 | 2001-02-08 | Ammonia Casale Sa | Verfahren zur Nachrüstung eines heterogenen exothermischen Synthesereaktors |
DE4446359A1 (de) * | 1993-12-29 | 1995-07-06 | Ammonia Casale Sa | Verfahren zur in-situ-Modernisierung eines heterogenen exothermen Synthesereaktors, insbesondere eines sogenannten Kellog-Reaktors |
RU95100777A (ru) * | 1994-01-20 | 1996-10-27 | Метанол Казале С.А. (Ch) | Способ модернизации на месте реактора для проведения гетерогенных экзотермических реакций синтеза, в частности, реактора, так называемого ромбовидного типа и реактор для его осуществления |
DE4439807A1 (de) * | 1994-11-08 | 1996-05-09 | Basf Ag | Reaktor zur Durchführung heterogenkatalysierter Gasphasenreaktionen |
ZA962804B (en) * | 1995-04-11 | 1996-07-29 | Floriall Holdings Ltd | Process and reactor for heterogeneous exothermic synthesis of formaldehyde |
US5986146A (en) * | 1995-04-11 | 1999-11-16 | Floriall Holdings Limited | Process and reactor for heterogeneous exothermic synthesis of formaldehyde |
CN1088618C (zh) * | 1996-08-21 | 2002-08-07 | 楼寿林 | 一种接近最佳温度的催化反应改进工艺及其合成反应器 |
DE69732781T2 (de) | 1997-11-28 | 2006-02-02 | Ammonia Casale S.A. | Verfahren zur in-situ Modernisierung eines heterogenen exothermen Synthesereaktors |
US6132687A (en) * | 1998-05-21 | 2000-10-17 | Kellogg Brown & Root, Inc. | Horizontal ammonia converter adapted for high activity catalyst |
EP1080778B1 (en) * | 1999-08-31 | 2003-07-23 | Ammonia Casale S.A. | Method for modernization of a heterogeneous synthesis reactor |
US20020183571A1 (en) * | 2000-11-30 | 2002-12-05 | Sud-Chemie Inc. | Radial reactor loading of a dehydrogenation catalyst |
US7435862B2 (en) | 2000-11-30 | 2008-10-14 | Sud-Chemie Inc. | Radial reactor loading of a dehydrogenation catalyst |
GB0115243D0 (en) * | 2001-06-21 | 2001-08-15 | Kvaerner Process Tech Ltd | Method |
US7718137B2 (en) * | 2005-10-28 | 2010-05-18 | Eastman Chemical Company | Reactor with optimized internal tray design |
US7867460B2 (en) * | 2007-11-26 | 2011-01-11 | Kellogg Brown & Root Llc | Efficiency of ammonia processes |
US20100074389A1 (en) * | 2008-09-25 | 2010-03-25 | Ge-Hitachi Nuclear Energy Americas Llc | Replacement basket, a system using the replacement basket, and a method for loading the replacement basket |
EP2354092A1 (en) | 2010-01-29 | 2011-08-10 | Ammonia Casale S.A. | A method for modernizing the synthesis loop of an ammonia plant |
EA201990088A1 (ru) * | 2016-06-21 | 2019-05-31 | Хальдор Топсёэ А/С | Конвертер с осевым/радиальным потоком |
AR113648A1 (es) * | 2017-12-20 | 2020-05-27 | Haldor Topsoe As | Convertidor de flujo axial adiabático |
AR113649A1 (es) * | 2017-12-20 | 2020-05-27 | Haldor Topsoe As | Convertidor de flujo axial enfriado |
WO2023163798A1 (en) | 2022-02-23 | 2023-08-31 | SANsyco Consulting, LLC | Ammonia synthesis converter and method for small production units |
Family Cites Families (15)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DK106275C (da) * | 1963-09-28 | 1967-01-16 | Topsoe Haldor F A | Reaktor til udførelse af gasfasereaktioner ved heterogen katalyse. |
DK119652B (da) * | 1964-09-11 | 1971-02-08 | Topsoe H | Reaktør til udførelse af gasfasereaktioner ved gennemledning af en gasblanding gennem et leje fyldt med katalysatørpartikler. |
DE1667161C3 (de) * | 1968-02-08 | 1973-10-31 | Lentia Gmbh, Chem. U. Pharm. Erzeugnisse - Industriebedarf, 8000 Muenchen | Verfahren und Vorrichtung zur Gasführung in katalytischen Hochdruck syntheseanlagen |
US3918918A (en) * | 1972-03-15 | 1975-11-11 | Lummus Co | Catalytic reactor |
TR18747A (tr) * | 1975-07-15 | 1977-08-02 | Snam Progetti | Yueksek termik duezeyli buhar ueretimiyle amonyagin sentezine mahsus radyal akisli reaktoer |
GB1574723A (en) * | 1976-03-10 | 1980-09-10 | Haldor Topsoe As | Apparatus for the synthesis of ammonia |
US4230669A (en) * | 1978-07-17 | 1980-10-28 | Pullman Incorporated | Radial ammonia converter |
US4346060A (en) * | 1978-07-17 | 1982-08-24 | Pullman Incorporated | Radial ammonia converters |
US4230680A (en) * | 1978-07-17 | 1980-10-28 | Pullman Incorporated | Low energy process for synthesis of ammonia |
FR2460707B1 (fr) * | 1979-07-13 | 1986-09-05 | Ammonia Casale Sa | Reacteur de synthese, notamment pour la synthese catalytique d'ammoniac et de methanol |
IT1141102B (it) * | 1980-11-28 | 1986-10-01 | Ammonia Casale Sa | Reattore assiale-radiale per sintesi eterogenee |
CH646618A5 (it) * | 1981-03-26 | 1984-12-14 | Ammonia Casale Sa | Reattore per sintesi eterogenee catalitiche. |
JPS5959242A (ja) * | 1982-09-28 | 1984-04-05 | Toyo Eng Corp | 反応方法およびそのための反応器 |
US4518574A (en) * | 1983-03-07 | 1985-05-21 | Exxon Research & Engineering Co. | Catalytic gas synthesis process |
JPS60110328A (ja) * | 1983-11-17 | 1985-06-15 | Toyo Eng Corp | 接触反応装置 |
-
1986
- 1986-04-02 IN IN264/CAL/86A patent/IN165082B/en unknown
- 1986-04-10 DE DE3686783T patent/DE3686783T3/de not_active Expired - Lifetime
- 1986-04-10 EP EP86104911A patent/EP0202454B2/en not_active Expired - Lifetime
- 1986-05-02 US US06/859,044 patent/US4755362A/en not_active Expired - Lifetime
- 1986-05-13 CA CA000509060A patent/CA1277123C/en not_active Expired - Lifetime
- 1986-05-14 ES ES554947A patent/ES8703812A1/es not_active Expired
- 1986-05-14 UA UA4027473A patent/UA32508C2/uk unknown
- 1986-05-14 CN CN86103332.9A patent/CN1004611B/zh not_active Expired
-
1988
- 1988-06-24 US US07/210,868 patent/US4952375A/en not_active Expired - Lifetime
- 1988-07-01 US US07/214,582 patent/US4904453A/en not_active Expired - Lifetime
Also Published As
Publication number | Publication date |
---|---|
EP0202454A3 (en) | 1987-09-09 |
ES8703812A1 (es) | 1987-03-01 |
UA32508C2 (uk) | 2001-02-15 |
DE3686783T3 (de) | 1997-05-07 |
CN1004611B (zh) | 1989-06-28 |
IN165082B (zh) | 1989-08-12 |
US4904453A (en) | 1990-02-27 |
US4952375A (en) | 1990-08-28 |
EP0202454A2 (en) | 1986-11-26 |
EP0202454B2 (en) | 1997-03-05 |
DE3686783D1 (de) | 1992-10-29 |
US4755362A (en) | 1988-07-05 |
ES554947A0 (es) | 1987-03-01 |
CA1277123C (en) | 1990-12-04 |
EP0202454B1 (en) | 1992-09-23 |
DE3686783T2 (de) | 1993-05-06 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
CN86103332A (zh) | 改进非均相催化合成反应器以降低能量消耗的系统及其相应的反应器 | |
CN1031110C (zh) | 放热反应方法及所用设备 | |
CN1133630C (zh) | 用于高度放热反应的催化转化器和方法 | |
CN1166446C (zh) | 多相放热合成反应器的原位现代化方法 | |
CA1271019A (en) | Converter for heterogeneous synthesis more particularly for ammonia, methanol and higher alcohols | |
EP0297474B1 (en) | Improved process for heterogeneous synthesis and related reactors | |
CN1355724A (zh) | 反应器、特别是放热反应的反应器 | |
CN1305821C (zh) | 甲醇合成 | |
CN101367700B (zh) | 用于以含氧化合物为原料生产丙烯的径向移动床反应器 | |
CN1791459A (zh) | 化学反应器 | |
CN200955019Y (zh) | 合成多段径向冷激式反应器 | |
CN110201624A (zh) | 一种用于合成反应的连续分段进料反应器 | |
CN1184436A (zh) | 甲醛的多相放热合成的方法和反应器 | |
CN87104678A (zh) | 改善非均匀合成反应器中反应气体与骤冷气体混合的系统 | |
CN1109798A (zh) | 就地改造多相放热合成反应器、特别是凯洛格型反应器的方法 | |
CN1184437A (zh) | 甲醛的多相放热合成的方法和反应器 | |
CA1317094C (en) | System to improve the efficiency of reactors for exothermic synthesis and more particularly for the reaction of ammonia | |
CN2499385Y (zh) | 部分氧化制备合成气的径向反应器 | |
CN1224634A (zh) | 一种多相合成反应器的原位现代化方法 | |
WO1996007474A1 (en) | Method for in-situ modernization of a urea synthesis reactor | |
CN1039791C (zh) | 一种气固催化反应器 | |
EP0269854B1 (en) | Process for reducing energy consumption in multi-unit reactors for heterogeneoussynthesis and related reactors | |
CN218901792U (zh) | 一种二氧化碳加氢制甲醇用合成装置 | |
EP0075056A1 (en) | Synthesis system and process for the production of ammonia | |
CN2751016Y (zh) | 多床层轴径向复合床间接换热式节能型氨合成塔 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
C10 | Entry into substantive examination | ||
SE01 | Entry into force of request for substantive examination | ||
C06 | Publication | ||
PB01 | Publication | ||
C13 | Decision | ||
GR02 | Examined patent application | ||
C14 | Grant of patent or utility model | ||
GR01 | Patent grant | ||
C17 | Cessation of patent right | ||
CX01 | Expiry of patent term |