CN1259391C - Method of cracking heavy hydrocarbon to prepare low-carbon olefin and the cracking gasifier system - Google Patents
Method of cracking heavy hydrocarbon to prepare low-carbon olefin and the cracking gasifier systemDownload PDFInfo
- Publication number
- CN1259391C CN1259391CCN 200310100482CN200310100482ACN1259391CCN 1259391 CCN1259391 CCN 1259391CCN 200310100482CN200310100482CN 200310100482CN 200310100482 ACN200310100482 ACN 200310100482ACN 1259391 CCN1259391 CCN 1259391C
- Authority
- CN
- China
- Prior art keywords
- cracking
- gasification
- gas
- coke
- furnace
- 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
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
Translated fromChinese
Description
Translated fromChinese技术领域technical field
本发明涉及一种裂解制取低碳烯烃的方法，特别是涉及一种采用重质烃直接裂解，以制取乙烯为主，并联产合成气(CO+H2)和丙烯、丁烯等低碳烯烃的重质烃裂解制取低碳烯烃的方法及裂解气化炉系统。The present invention relates to a cracking method for producing low-carbon olefins, in particular to a method for direct cracking of heavy hydrocarbons, mainly for producing ethylene, and co-producing synthesis gas (CO+H2 ) and propylene, butene, etc. A method for producing light olefins by cracking heavy hydrocarbons of light olefins and a cracking gasifier system.
背景技术Background technique
管式炉高温裂解法是乙烯生产的主流方法，目前世界上采用此法生产的乙烯高达乙烯总产量的99％以上。管式炉高温裂解法最主要的工艺参数是高温、短停留时间和低的烃分压，裂解原料包括石脑油、轻柴油、液化石油气、乙烷等轻质石油烃，其中又以石脑油和乙烷为最主要的原料来源。据统计，全球产自这两种原料的乙烯超过乙烯总产量的75％，如文献[1]崔静怡.乙烯原料发展趋势及优化建议.石油化工技术经济.2001，17(6).中所介绍的。我国乙烯的市场需求和生产能力的持续快速增长，使原本紧张的轻质烃原料的供需矛盾日趋突出。The tube furnace pyrolysis method is the mainstream method of ethylene production. At present, the ethylene produced by this method is as high as 99% of the total ethylene production in the world. The main process parameters of the tube furnace pyrolysis method are high temperature, short residence time and low hydrocarbon partial pressure. The cracking raw materials include light petroleum hydrocarbons such as naphtha, light diesel oil, liquefied petroleum gas, and ethane. Naphtha and ethane are the main sources of raw materials. According to statistics, the ethylene produced from these two raw materials in the world exceeds 75% of the total ethylene production, as described in [1] Cui Jingyi. The development trend and optimization suggestions of ethylene raw materials. Petrochemical Technology Economics. 2001, 17 (6). of. The continuous and rapid growth of my country's ethylene market demand and production capacity has made the contradiction between supply and demand of light hydrocarbon raw materials that were originally tense increasingly prominent.
我国多年来持续努力的一个方面是希望将重质烃(原油、重油、渣油或聚烯烃废塑料等)作为乙烯生产的裂解原料。重质烃裂解需要更高的裂解温度，管式炉因存在炉管材质和操作方面的困难，使之难以成为重质烃的裂解设备。高温下炉管抗蠕变性能降低将缩短炉管的使用寿命，重质烃裂解时更易在炉管内壁结焦，增大了炉管的传热和流动阻力。One aspect of my country's continuous efforts over the years is to use heavy hydrocarbons (crude oil, heavy oil, residual oil or polyolefin waste plastics, etc.) as cracking raw materials for ethylene production. The cracking of heavy hydrocarbons requires a higher cracking temperature, and tube furnaces are difficult to use as cracking equipment for heavy hydrocarbons due to the difficulties in furnace tube material and operation. The reduced creep resistance of the furnace tube at high temperature will shorten the service life of the furnace tube, and it is easier to coke on the inner wall of the furnace tube when heavy hydrocarbons are cracked, which increases the heat transfer and flow resistance of the furnace tube.
我国曾研究非管式炉重质烃裂解工艺，其中的典型代表为蓄热炉裂解工艺和砂子炉裂解工艺。蓄热炉裂解法由于热利用效率低，环境污染大，能耗高等多方面原因，经济上缺乏竞争性；砂子炉法操作复杂、设备磨损严重、热回收效率低、废砂难于处理；这两种工艺，近年来均未得到进一步的发展而逐渐被废弃，如文献[2]：曾清泉.乙烯.化工百科全书(18).北京：化学工业出版社.1998.866-867。Our country has studied non-tube furnace heavy hydrocarbon cracking process, and the typical representatives are regenerative furnace cracking process and sand furnace cracking process. The regenerative furnace cracking method is economically uncompetitive due to low heat utilization efficiency, high environmental pollution, and high energy consumption; the sand furnace method is complex in operation, serious in equipment wear, low in heat recovery efficiency, and difficult to dispose of waste sand; these two This process has not been further developed in recent years and has been gradually abandoned, such as literature [2]: Zeng Qingquan. Ethylene. Encyclopedia of Chemical Engineering (18). Beijing: Chemical Industry Press. 1998.866-867.
全氧高炉作为炼铁设备具有在同一反应器中进行反应和供热，热效率高的特点，高炉的炉膛设计使之既能承受高温，又无结焦堵塞管路之虞。在高炉的适当位置增加原料和产物的出、入口，可改造为能满足重质烃裂解制取低碳烯烃工艺要求的裂解气化炉。重质烃裂解疏松的结焦，可充氧燃烧供热，同时联产合成气(CO+H2)。随着钢铁工业高炉大型化的进程，我国将有许多现代化的退役高炉，如将其改造为重质烃裂解制取低碳烯烃并联产合成气的裂解气化炉，不失为中小规模的钢铁企业提供了一条出路。Oxygen blast furnace as an ironmaking equipment has the characteristics of reaction and heat supply in the same reactor, and high thermal efficiency. The furnace design of the blast furnace can withstand high temperature without the risk of coking and blocking the pipeline. Adding inlets and outlets of raw materials and products at appropriate positions of the blast furnace can be transformed into a cracking gasifier that can meet the process requirements for producing low-carbon olefins by cracking heavy hydrocarbons. Heavy hydrocarbon cracking loose coke can be used for oxygen-charged combustion for heating and co-production of synthesis gas (CO+H2 ). With the process of large-scale blast furnaces in the iron and steel industry, there will be many modern decommissioned blast furnaces in my country, such as cracking gasifiers for producing low-carbon olefins and co-producing syngas by cracking heavy hydrocarbons, which can be regarded as small and medium-sized iron and steel enterprises. Provided a way out.
发明内容：Invention content:
本发明的目的在于克服已有的管式炉工艺难以裂解重质烃、蓄热炉工艺热利用和生产效率低、砂子炉工艺设备磨损严重和废砂排放多的技术缺陷，为了有效地利用我国的石油资源，来制取最基本的有机化工基础原料，从而提供了一种重质烃裂解清洁制取乙烯等低碳烯烃的方法和裂解气化炉系统。The purpose of the present invention is to overcome the technical defects that the existing tubular furnace process is difficult to crack heavy hydrocarbons, the heat utilization and production efficiency of the regenerative furnace process is low, the sand furnace process equipment is seriously worn and the waste sand is discharged, in order to effectively utilize my country's Petroleum resources to produce the most basic organic chemical raw materials, thus providing a method of cracking heavy hydrocarbons to cleanly produce low-carbon olefins such as ethylene and a cracking gasifier system.
本发明的目的是这样实现的：The purpose of the present invention is achieved like this:
本发明提供的裂解气化炉系统，包括冶金高炉1为主体，其底部为炉缸16，高炉1的气体出口14通过管道15与余热锅炉3连通；其特征在于：所述的高炉1炉体分为三段，其中下段为燃烧区8，该燃烧区8处在炉体1/5～2/5与炉缸16之间，其上1/5～3/5高度为气化裂解区9，气化裂解区9以上部分为气化完成区10；在燃烧区8和气化裂解区9的炉体壁上开有第一气体入口12和第二气体入口13，在气化完成区10的炉体壁上开有一气体出口14，在第一气体入口12上连通水蒸汽和氧气管道，第二气体入口13上连通重质烃和水蒸汽管道。The pyrolysis gasification furnace system provided by the present invention comprises a
还包括余热锅炉3的气体出口与一净化单元4、压缩单元5、冷箱单元6和分离单元7通过管道顺序连通。It also includes a gas outlet of the
还包括在冷箱单元6的输出管道与第二气体入口13连通，余热锅炉3的另一气体出口也与第一气体入口12连通。It also includes that the output pipe of the
还包括分离单元7的输出管道与冷箱单元6的冷流入口连通。It also includes the output pipe of the separation unit 7 communicating with the cold flow inlet of the
其中净化单元4可以是脱硫除尘器；其中压缩单元5可以是气体压缩机；其中分离单元7可以为气液分离器。Wherein the
所述的冶金高炉包括：钢铁企业的退役炼钢、炼铁高炉或其它高炉。The metallurgical blast furnace includes: decommissioned steelmaking, ironmaking blast furnaces or other blast furnaces of iron and steel enterprises.
本发明提供的重质烃裂解制取低碳烯烃的方法，包括以下步骤：The method for producing light olefins by cracking heavy hydrocarbons provided by the invention comprises the following steps:
1.首先在本发明的裂解气化炉内填充焦炭或半焦床层，该填充床层的下部为燃烧区8，占整个床层的1/5～2/5，为重质烃裂解提供所需要的热量，该填充床层的中部为气化裂解区9，占整个床层的1/5～3/5，上部为气化完成区10，占整个床层的1/5～3/5；1. First fill coke or semi-coke bed in cracking gasifier of the present invention, the bottom of this packed bed is
2.点火开炉；2. Ignite and start the furnace;
3.点火后向燃烧区8的焦炭床层通入氧气和水蒸汽，流速为0.9～15m3/s，水蒸汽和氧气的体积比为3～7∶1，将焦炭床层烧至炽热状态；通入的氧气用于焦炭的燃烧，以提供裂解反应所需要的热量，通入的水蒸汽用以控制焦炭燃烧的火焰温度，使之温度保持在1573～2073K(1300～1800℃)之间；3. After ignition, feed oxygen and water vapor into the coke bed in the
4.当温度保持在1573～2073K(1300～1800℃)之间时，通过第二气体入口向气化裂解区9的焦炭床层喷入经预热并雾化的重质烃和水蒸汽，或者向炉内添加固体裂解原料，该原料可以经破碎后加入，所述的喷入经预热并雾化的重质烃与过程水蒸汽重量比为1∶0.75～10，添加量为单位时间内重质烃的进料量为0.2～50kg/s；燃烧区的焦炭燃烧产物和水蒸汽与气化裂解区的焦炭发生反应，部分焦炭被气化产生合成气；重质烃在通入裂解气化炉的过程中被强烈加热，至焦炭表面裂解；通入的水蒸汽在作为焦炭气化反应原料的同时，作为烃类裂解反应的稀释剂；4. When the temperature is kept between 1573～2073K (1300～1800°C), spray preheated and atomized heavy hydrocarbons and water vapor into the coke bed in the
5.裂解和气化产物进入气化完成区10，以流出速度为1～350m3/s，或0.5～200kg/s导出裂解气化炉，使得重质烃在裂解气化炉中的停留时间为0.01～0.5s，经余热锅炉3回收热量。5. The cracking and gasification products enter the
还包括步骤6：经余热锅炉3回收热量送至净化单元4；经过净化的气体再经压缩单元5压缩后，用冷箱单元6和分离单元7分离裂解和气化产物。It also includes step 6: the heat recovered by the
所述的原料可以用原油、重油和渣油，也可以是聚烯烃废塑料等。The raw material can be crude oil, heavy oil and residual oil, or polyolefin waste plastics and the like.
还包括从重质烃的裂解和气化产物中可以分离出乙烯、丙烯、液化石油气、合成气(CO+H2)等，经冷凝产生的液态裂解油可以作为原料再返回裂解气化炉，进一步裂解制取低碳烯烃，也可以加氢后制成成品油。It also includes that ethylene, propylene, liquefied petroleum gas, synthetic gas (CO+H2 ) can be separated from the cracking and gasification products of heavy hydrocarbons, and the liquid cracking oil produced by condensation can be used as raw material and then returned to the cracking gasifier for further It can be cracked to produce low-carbon olefins, and can also be hydrogenated to produce refined oil.
还包括在裂解气化炉中裂解产生的结焦沉积于焦炭表面，在下部氧气的作用下转化为热量，或与水蒸汽和来自燃烧区的燃烧产物发生反应，产生合成气，补充(或部分补充)焦炭的消耗。It also includes the deposition of coke produced by cracking in the cracking gasifier on the surface of coke, which is converted into heat under the action of oxygen in the lower part, or reacts with water vapor and combustion products from the combustion zone to produce syngas, supplemented (or partially supplemented) ) Coke consumption.
所述的步骤4中的重质烃预热至323～623K(50～350℃)，水蒸汽预热至623～923K(350～650℃)。In the
本发明将重质烃(原油、重油、渣油或聚烯烃废塑料等)的裂解和供热整合在同一反应器中，通过控制氧气流速和氧气与水蒸汽的配比，控制焦炭的氧化速率和裂解温度的方法和装置，其优点在于：The present invention integrates the cracking and heat supply of heavy hydrocarbons (crude oil, heavy oil, residual oil or polyolefin waste plastics, etc.) in the same reactor, and controls the oxidation rate of coke by controlling the oxygen flow rate and the ratio of oxygen to water vapor And the method and device of pyrolysis temperature, its advantage is:
(1)热效率高，满足烃类裂解短时间内大量供热的工艺要求；(1) High thermal efficiency, meeting the technical requirements of a large amount of heat supply in a short period of time for hydrocarbon cracking;
(2)通过调节氧气流速，可以控制焦炭床层的氧化速率，通过调整氧气与水蒸汽的比例，可以控制焦炭床层的火焰温度；(2) By adjusting the oxygen flow rate, the oxidation rate of the coke bed can be controlled, and by adjusting the ratio of oxygen to water vapor, the flame temperature of the coke bed can be controlled;
(3)配合适宜的重质烃喷入流速和裂解产物的导出流速，可以控制裂解反应的停留时间，使短停留时间的工艺要求成为可能；(3) Cooperating with the appropriate heavy hydrocarbon injection flow rate and the export flow rate of the cracked product, the residence time of the cracking reaction can be controlled, making it possible to meet the technological requirements of short residence time;
(4)裂解炉中的高温和较高的气体流速，配合一定比例的水蒸汽，使较低烃分压的工艺要求成为可能；(4) The high temperature and high gas flow rate in the cracking furnace, combined with a certain proportion of water vapor, make the process requirements of lower hydrocarbon partial pressure possible;
(5)裂解产生的结焦沉积于焦炭表面，在氧气的作用下发生强烈的氧化反应并转化为热量，或与水蒸汽和二氧化碳反应而气化，避免了裂解设备结焦后频繁清焦的操作；(连续的结焦、烧焦和气化过程，为连续的重质烃裂解提供了热量条件，提高了重质烃的裂解效率，降低了添加焦炭操作的频度和裂解操作的复杂性)；(5) The coke produced by cracking is deposited on the coke surface, and under the action of oxygen, a strong oxidation reaction occurs and is converted into heat, or reacts with water vapor and carbon dioxide to gasify, avoiding the frequent coke cleaning operation after the cracking equipment is coked; (Continuous coking, coking and gasification processes provide thermal conditions for continuous cracking of heavy hydrocarbons, improve the cracking efficiency of heavy hydrocarbons, reduce the frequency of coke addition operations and the complexity of cracking operations);
(6)裂解气化炉底部的炉缸结构，使重质烃中的无机成分在高温下与加入的熔剂石灰石形成炉渣，从裂解气化炉的渣口排出，避免了如砂子炉大量排放黑色焦砂而造成的污染。(6) The furnace hearth structure at the bottom of the pyrolysis gasifier enables the inorganic components in heavy hydrocarbons to form slag with the added flux limestone at high temperature, and is discharged from the slag port of the cracking gasifier, avoiding a large amount of black discharge such as a sand furnace pollution caused by scorched sand.
本发明以钢铁企业的退役高炉为基础，在高炉的适当位置增加原料和产物的出、入口，可改造为裂解气化炉；以裂解气化炉内填充的焦炭作为热源和热载体，直接燃烧提供烃类裂解所需的热量，以重质烃(原油、重油、渣油或聚烯烃废塑料等)为裂解原料，以氧气和水蒸汽为助剂，使重质烃在炉内发生裂解反应，制取乙烯等低碳烯烃，同时可联产合成气(CO+H2)；裂解反应形成的结焦可补充(或部分补充)焦炭的消耗。The present invention is based on the decommissioned blast furnace of the iron and steel enterprise, and the inlet and outlet of raw materials and products are added at the appropriate position of the blast furnace, which can be transformed into a cracking gasifier; the coke filled in the cracking gasifier is used as the heat source and heat carrier for direct combustion Provide the heat required for the cracking of hydrocarbons, use heavy hydrocarbons (crude oil, heavy oil, residual oil or polyolefin waste plastics, etc.) , to produce low-carbon olefins such as ethylene, and simultaneously produce syngas (CO+H2 ); the coke formed by the cracking reaction can supplement (or partially supplement) the consumption of coke.
本发明涉及重质烃(原油、重油、渣油或聚烯烃废塑料等)的裂解，(1)除裂解原料外，焦炭、氧气和水蒸汽也参与反应，水蒸汽在裂解工艺过程中同时还具有稀释裂解产物的作用；(2)裂解产物有低碳烯烃、低碳烷烃、合成气(CO+H2)等气态产物，也有可冷凝为裂解油的液态产物，还有结焦反应产生的固态产物；(3)气态产物(包括出口温度下的裂解油)导出裂解炉，回收热量后经气体分离装置，可分离出乙烯、丙烯、液化石油气、合成气(CO+H2)等，冷凝可能产生的液态裂解油可返回裂解炉再次裂解或加氢后制成成品油，裂解的结焦用于供热或产生合成气；(4)该工艺除排出炉渣固体废弃物外，可以很少甚至不排放污染物，对环境基本无污染。The present invention relates to the pyrolysis of heavy hydrocarbons (crude oil, heavy oil, residual oil or polyolefin waste plastics, etc.), (1) In addition to the cracking raw materials, coke, oxygen and water vapor also participate in the reaction, and the water vapor is also returned during the cracking process It has the function of diluting the cracking products; (2) The cracking products include gaseous products such as low-carbon olefins, low-carbon alkanes, and synthesis gas (CO+H2 ), as well as liquid products that can be condensed into cracked oil, and solids produced by coking reactions products; (3) gaseous products (including cracked oil at the outlet temperature) are exported to the cracking furnace, and after recovering heat, they can be separated from ethylene, propylene, liquefied petroleum gas, synthetic gas (CO+H2 ), etc., and condensed The liquid cracked oil that may be produced can be returned to the cracking furnace to be cracked again or hydrogenated to make refined oil, and the cracked coke can be used for heating or generating synthesis gas; No pollutants are emitted, and there is basically no pollution to the environment.
附图说明Description of drawings
图1是本发明的裂解气化炉系统结构示意图Fig. 1 is the structural representation of cracking gasification furnace system of the present invention
图2是在本发明的裂解炉中利用本发明方法的综合利用工艺流程示意图Fig. 2 is a schematic diagram of the comprehensive utilization process flow utilizing the method of the present invention in the cracking furnace of the present invention
图3是本发明气化裂解方法的工艺流程示意图Fig. 3 is the technological process schematic diagram of gasification cracking method of the present invention
图面说明Illustration
1-高炉 2-焦炭入口 3-余热锅炉1- Blast furnace 2- Coke inlet 3- Waste heat boiler
4-净化单元 5-压缩单元 6-冷箱单元4-Purification unit 5-Compression unit 6-Cold box unit
7-分离单元 8-燃烧区 9-气化裂解区7-Separation unit 8-Combustion zone 9-Gasification cracking zone
10-气化完成区 11-排渣口 12-第一气体入口10-gasification completion area 11-slag outlet 12-first gas inlet
13-第二气体入口 14-气体出口 15-管道13-Second gas inlet 14-Gas outlet 15-Pipeline
16-炉缸16-hearth
具体实施方式Detailed ways
下面结合附图和实施例对本发明进行详细的说明。The present invention will be described in detail below in conjunction with the accompanying drawings and embodiments.
实施例1Example 1
参考图1，本实施例用一冶金高炉，特别是可以采用钢铁企业的退役高炉1为主体进行改造，在其底部为炉缸16，所述的裂解气化炉炉体分为三段，炉缸16之上至炉体1/5处为燃烧区8，在炉体1/5～3/5高度以下为气化裂解区9，该气化裂解区以上部分为气化完成区10；在燃烧区8炉体壁上开有第一气体入口12，和气化裂解区9的炉体壁上开有第二气体入口13，在气化完成区10的炉体壁上开有一气体出口14，其气体出口14通过管道15与余热锅炉3连通；在第一气体入口12连通水蒸汽和氧气管道，第二气体入口13连通重质烃和水蒸汽管道。With reference to Fig. 1, the present embodiment uses a metallurgical blast furnace, especially the decommissioned
参考图2Refer to Figure 2
本实施例还包括在图1的钢铁企业的退役高炉1为主体和余热锅炉3制作的的裂解炉上再增加：净化单元4、压缩单元5、冷箱单元6和分离单元7；其中气体出口14与一脱硫除尘器4、气体压缩机5、冷箱6和气液分离器7通过管道顺序连通；冷箱6和气液分离器7的输出管道与第二气体入口13连通，余热锅炉3的气体出口与第一气体入口12连通。本实施例中还可以使用其他冶金高炉1为主体；冷箱单元6采用杭州制氯机厂生产的冷箱。Present embodiment also includes adding on the pyrolysis furnace that the decommissioned
实施例2Example 2
本实施例的重质烃裂解制取低碳烯烃的方法是在实施例1的气化裂解炉中进行的，其具体实施步骤如下：The method for producing light olefins by cracking heavy hydrocarbons of the present embodiment is carried out in the gasification cracking furnace of
(1)在实施例1制作的裂解气化炉内填充焦炭或半焦床层，该填充床层的下部为燃烧区8，占整个床层的1/5，为重质烃裂解提供所需要的热量，该填充床层的中部为气化裂解区9，占整个床层的2/5，上部为气化完成区10，占整个床层的2/5；(1) Fill coke or semi-coke bed in the pyrolysis gasifier that
(2)点火开炉；(2) ignite and start the furnace;
(3)向燃烧区8的焦炭床层通入氧气和水蒸汽，流速为1.4m3/s，水蒸汽和氧气的体积比为5∶1，将焦炭床层烧至炽热状态；通入的氧气用于焦炭的燃烧，以提供裂解反应所需要的热量，通入的水蒸汽用以控制焦炭燃烧的火焰温度，使之略低于2073K(1800℃)；(3) Oxygen and water vapor are fed into the coke bed in the
(4)向气化裂解区9的焦炭床层喷入经预热并雾化的重质烃和水蒸汽，重质烃预热至383K(110℃)，水蒸汽预热至723K(450℃)，重质烃与过程蒸汽重量比为1∶1，单位时间内重质烃的进料量为0.278kg/s；燃烧区8的焦炭燃烧产物和水蒸汽与气化裂解区的焦炭发生反应，部分焦炭被气化产生合成气；重质烃在通入裂解气化炉的过程中被强烈加热，至焦炭表面裂解；通入的水蒸汽在作为焦炭气化反应原料的同时，作为烃类裂解反应的稀释剂；(4) Spray preheated and atomized heavy hydrocarbons and steam into the coke bed in the
(5)裂解和气化产物进入气化完成区10，快速导出裂解气化炉，流速为2m3/s标准态体积，经余热锅炉3回收热量后，送至净化单元4；(5) The pyrolysis and gasification products enter the
(6)气体经压缩单元5压缩后，用冷箱单元6和分离单元7分离裂解和气化产物。(6) After the gas is compressed by the
本发明通入的是纯氧，裂解气化炉的气化完成区出口气的组成列于表1。What the present invention feeds is pure oxygen, and the composition of the outlet gas of the gasification completion zone of the cracking gasifier is listed in Table 1.
在同等的操作条件下，以蓄热炉裂解山东原油所得的裂解气组成结果也示于表1。Under the same operating conditions, the cracked gas composition results obtained from cracking Shandong crude oil with the regenerative furnace are also shown in Table 1.
表1 山东原油裂解气全分析数据(体积％)
本发明采用全氧技术，代替文献5：丹阳县化肥厂.石油化工.1975，4(增刊)：2-9.中的空气，促进焦炭的燃烧。The present invention adopts all-oxygen technology to replace the air in document 5: Danyang Fertilizer Factory. Petrochemical Industry. 1975, 4 (Supplement): 2-9. to promote the combustion of coke.
其中蓄热炉裂解山东原油的操作条件为文献5记载的条件：原油预热至383K(110℃)，雾化油压10kg/cm2，原油与过程蒸汽比为1∶1，水蒸汽温度为723K(450℃)，压力为4.5kg/cm2，通入一定量的空气，裂解温度为1073K(800℃)。Among them, the operating conditions of regenerative furnace cracking Shandong crude oil are the conditions recorded in Document 5: crude oil is preheated to 383K (110°C), atomized oil pressure is 10kg/cm2 , the ratio of crude oil to process steam is 1:1, and the steam temperature is 723K (450°C), the pressure is 4.5kg/cm2 , a certain amount of air is introduced, and the cracking temperature is 1073K (800°C).
实施例3Example 3
在实施例1制作的裂解气化炉内，按图2综合利用的工艺流程图进行，该裂解气化炉的进料包括氧气、水蒸汽和裂解原料，其中大部分水蒸汽的来源是从余热锅炉3换热而来的，裂解原料除了重质烃外，部分来自冷箱单元6和分离单元7返回的甲烷、乙烷等低碳烷烃作为原料。In the pyrolysis gasifier made in
裂解气化炉的气体出口14的温度为1073～1173K(800～900℃)，裂解和气化产物通入余热锅炉，经热量回收后，气体温度降低为573K(300℃)以下。与此同时，用于制冷的水吸热转变为水蒸汽，导入裂解气化炉参与反应。The temperature of the
从余热锅炉3出来的裂解气化产物经脱硫除尘器(净化单元4)净化后，送入气体压缩机5，经压缩后的气体产物，与输入的一定量的冷量一起进入冷箱单元6进行分离，依照各组分沸点的不同而先后液化分离。各液态成分所携带的冷量，再次经过冷箱的换热器释放掉所携带的大部分冷量，用于从气体压缩机5输入的裂解气化产物的冷却分离。The pyrolysis gasification product from the
自冷箱分离而得到的气体组分，有合成气(CO+H2)、低碳烯烃、低碳烷烃等，其中合成气(CO+H2)和低碳烯烃分离作为化工原料，低碳烷烃如甲烷、乙烷等烷烃组分返回裂解气化炉后作为裂解原料再次裂解。The gas components separated from the cold box include synthesis gas (CO+H2 ), low-carbon olefins, and low-carbon alkanes, among which the synthesis gas (CO+H2 ) and low-carbon olefins are separated as chemical raw materials Alkanes such as methane, ethane and other alkane components are returned to the cracking gasifier and used as cracking raw materials for cracking again.
经过此过程的物料循环和能量再利用，在进一步提高低碳烯烃的收率的同时，使工艺过程中所产生的热量和冷量返回过程为过程所用，符合现代化化工工艺过程的要求，能够实现工艺过程中物质和能量最大限度的利用。Through material circulation and energy reuse in this process, while further increasing the yield of low-carbon olefins, the heat and cold generated in the process can be returned to the process for use, which meets the requirements of modern chemical processes and can realize Maximize the use of material and energy in the process.
依照此综合利用工艺，采用砂子炉原油裂解的操作条件所得出口气组成结果列于表2。According to this comprehensive utilization process, the composition results of the outlet gas obtained by using the sand furnace crude oil cracking operating conditions are listed in Table 2.
砂子炉原油裂解的操作条件如文献：山西省燃料化学研究所.石油化工.1975，4(1)：18-27.所述的：原油进料量为1100kg/h，原油与水蒸汽比为1∶1.15，裂解温度为1013K(740C)，停留时间为0.498s。其出口气组成结果也列于表2，以示对照。The operating conditions of sand furnace crude oil cracking are as document: Shanxi Institute of Fuel Chemistry. Petrochemical Industry. 1975, 4 (1): 18-27. Described: the feed rate of crude oil is 1100kg/h, and the ratio of crude oil and water vapor is 1:1.15, the cracking temperature is 1013K (740C), and the residence time is 0.498s. The composition of the outlet gas is also listed in Table 2 for comparison.
表2 原油裂解出口气体产物组成结果(体积％)
Claims (8)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200310100482CN1259391C (en) | 2003-10-17 | 2003-10-17 | Method of cracking heavy hydrocarbon to prepare low-carbon olefin and the cracking gasifier system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200310100482CN1259391C (en) | 2003-10-17 | 2003-10-17 | Method of cracking heavy hydrocarbon to prepare low-carbon olefin and the cracking gasifier system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1609169A CN1609169A (en) | 2005-04-27 |
| CN1259391Ctrue CN1259391C (en) | 2006-06-14 |
Family
ID=34755979
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200310100482Expired - Fee RelatedCN1259391C (en) | 2003-10-17 | 2003-10-17 | Method of cracking heavy hydrocarbon to prepare low-carbon olefin and the cracking gasifier system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1259391C (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101451702B (en)* | 2007-11-30 | 2011-04-20 | 上海吴泾化工有限公司 | Cracking gas heat comprehensive utilization method and exhaust heat boiler using the method |
| WO2012034295A1 (en)* | 2010-09-17 | 2012-03-22 | 林月蓉 | Apparatus and method for preparing lower olefin by cracking reaction |
Families Citing this family (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101865457B (en)* | 2009-04-16 | 2012-05-30 | 东莞市中拓节能科技有限公司 | Circulating fluidized bed boiler |
| CN102382667B (en)* | 2010-09-01 | 2013-12-25 | 中国石油化工股份有限公司 | Coal cracking and heavy oil cracking joint production method |
| CN103864556A (en)* | 2012-12-13 | 2014-06-18 | 中国科学院大连化学物理研究所 | Method for production of low carbon olefins from synthetic gas via low carbon alkanes |
| CN104232147B (en)* | 2013-06-21 | 2016-04-13 | 中国科学院过程工程研究所 | A kind of heavy oil lightweight treatment technique |
| CN105586067B (en)* | 2014-10-21 | 2018-04-24 | 中国科学院过程工程研究所 | Oxyhydrogen combustion method directly heats the device and method of oil pyrolysis hydrocarbon |
| CN108097188B (en)* | 2017-12-26 | 2019-09-20 | 杭州左纳实业有限公司 | The gasification installation of plasma pyrolysis residual oil and exhaust gas |
| US12031091B2 (en) | 2019-05-24 | 2024-07-09 | Eastman Chemical Company | Recycle content cracked effluent |
| WO2020242912A1 (en) | 2019-05-24 | 2020-12-03 | Eastman Chemical Company | Blend small amounts of pyoil into a liquid stream processed into a gas cracker |
| CN114206820B (en)* | 2019-07-29 | 2024-05-10 | 伊士曼化工公司 | Recovery of component (C)4) Alkanals and aldehydes |
| CN112538371B (en)* | 2019-09-23 | 2022-02-25 | 中国石油大学(北京) | A heavy oil lightening coupled reaction device |
| US11319262B2 (en) | 2019-10-31 | 2022-05-03 | Eastman Chemical Company | Processes and systems for making recycle content hydrocarbons |
| US11945998B2 (en) | 2019-10-31 | 2024-04-02 | Eastman Chemical Company | Processes and systems for making recycle content hydrocarbons |
| WO2021087057A1 (en) | 2019-10-31 | 2021-05-06 | Eastman Chemical Company | Pyrolysis method and system for recycled waste |
| CN120209878A (en)* | 2019-10-31 | 2025-06-27 | 伊士曼化工公司 | Pyrolysis method and system for recycling waste |
| US11939534B2 (en) | 2019-11-07 | 2024-03-26 | Eastman Chemical Company | Recycle content alpha olefins and fatty alcohols |
| CN114641465B (en) | 2019-11-07 | 2024-12-31 | 伊士曼化工公司 | Recycled ingredients mixed esters and solvents |
| US12195674B2 (en) | 2021-09-21 | 2025-01-14 | Eastman Chemical Company | Using spent caustic solution from pygas treatment to neutralize halogens from liquified waste plastic |
| CN116832878A (en)* | 2023-06-09 | 2023-10-03 | 大连理工大学 | An oxygen-rich regeneration method for light hydrocarbon cracking catalyst |
- 2003
- 2003-10-17CNCN 200310100482patent/CN1259391C/ennot_activeExpired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101451702B (en)* | 2007-11-30 | 2011-04-20 | 上海吴泾化工有限公司 | Cracking gas heat comprehensive utilization method and exhaust heat boiler using the method |
| WO2012034295A1 (en)* | 2010-09-17 | 2012-03-22 | 林月蓉 | Apparatus and method for preparing lower olefin by cracking reaction |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1609169A (en) | 2005-04-27 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1259391C (en) | Method of cracking heavy hydrocarbon to prepare low-carbon olefin and the cracking gasifier system | |
| CN102465043B (en) | Multi-section fractional pyrolysis gasification device and method for solid fuel | |
| CN108424785B (en) | Alkaline millisecond catalytic cracking and gasification coupling process for double reaction tubes of inferior heavy oil | |
| JP2004534903A (en) | How to create clean energy from coal | |
| CN108587674B (en) | Millisecond pyrolysis-gasification coupling process for heavy oil double-reaction tube semicoke circulating bed | |
| CN102115675A (en) | Heavy oil lightening method and device | |
| CN1782037A (en) | Apparatus and method for coal gasification | |
| CN103450922B (en) | Heavy oil thermal conversion and green coke gasification method and combined device | |
| CN102911686B (en) | Coal destructive distillation method and apparatus | |
| CN108531220A (en) | A kind of system and method for biomass microwave pyrolysis high yield gas | |
| CN102234522A (en) | Processing method and apparatus for converting heavy oil to light fractions | |
| CN105129800B (en) | A kind of oxygen/coal injection prepares the technique and system of calcium carbide and ethene | |
| CN204981160U (en) | System for oxygen / coal jetting preparation carbide and ethylene | |
| CN102031135A (en) | Comprehensive processing and utilizing method for heavy oil | |
| CN202912908U (en) | Heavy oil thermal cracking and gasification coupled double reaction tube circulating bed device | |
| CN110283609B (en) | Pyrolysis-coking combined process and system for preparing coal tar by pyrolyzing pulverized coal | |
| CN206266493U (en) | The system that a kind of coal is classified dual treatment | |
| CN105694936A (en) | Full-particle oil shale refining system and process | |
| CN104946282B (en) | A kind of handling process of smalls | |
| CN104945215A (en) | Method and system for preparing ethylene from powdered coal | |
| CN1418935A (en) | Method for preparing synthesis gas using natural gas and coal as raw material and furnace for preparing same | |
| CN113477186B (en) | A kind of heavy tar selective catalytic upgrading device and method thereof | |
| CN204981692U (en) | System for fine coal preparation ethylene | |
| CN105985804B (en) | A kind of mink cell focus processing technology and processing unit (plant) | |
| CN210656802U (en) | Hydrocarbon material pyrolysis and gasification coupling device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| 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:20060614 Termination date:20131017 |