CN101628198A - Pressure-swing adsorption method of directly enriching methane from coal bed gas - Google Patents
Pressure-swing adsorption method of directly enriching methane from coal bed gas Download PDFInfo
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Abstract
一种煤层气直接富集甲烷的变压吸附方法，将煤层气通入多塔吸附装置，通过变压吸附技术，在吸附剂上吸附N2，在出口直接富集CH4。还包括真空或降压解吸，实现吸附剂再生及循环使用。所述变压吸附工艺参数：充压吸附的压力控制在0.1～1MPa范围内；降压脱附的压力控制在0.1～0MPa范围内；温度控制在－80～120℃范围内。本工艺以孔口改性的4A、5A沸石分子筛及炭分子筛作为吸附剂，通过上述步骤，获得CH4的纯度达95％～99.9％。本发明比以往在吸附剂上富集CH4，通过降压解吸得到CH4产品气的工艺有明显优势，实现了低浓度抽放煤层气的综合利用，对保障煤矿安全生产、减少大气污染以及改善和优化我国能源结构具有重要意义。本工艺过程简单，操作方便，安全性能好，有利于大规模推广。
A pressure swing adsorption method for directly enriching methane from coalbed methane, in which coalbed methane is fed into a multi-tower adsorption device, N 2 is adsorbed on the adsorbent through pressure swing adsorption technology, and CH 4 is directly enriched at the outlet. It also includes vacuum or decompression desorption to realize the regeneration and recycling of the adsorbent. Said pressure swing adsorption process parameters: the pressure of pressure adsorption is controlled within the range of 0.1-1 MPa; the pressure of decompression desorption is controlled within the range of 0.1-0 MPa; the temperature is controlled within the range of -80-120°C. In this process, 4A, 5A zeolite molecular sieves and carbon molecular sieves modified by pores are used as adsorbents, and the purity of CH 4 obtained through the above steps reaches 95%-99.9%. Compared with the previous process of enriching CH 4 on the adsorbent and obtaining CH 4 product gas through decompression and desorption, the present invention has obvious advantages, and realizes the comprehensive utilization of low-concentration drained coalbed methane, which is helpful for ensuring safe production of coal mines, reducing air pollution and It is of great significance to improve and optimize China's energy structure. The process is simple, convenient to operate, good in safety performance, and conducive to large-scale popularization.
Description
技术领域 technical field
本发明涉及一种煤层气浓缩方法，属于气体分离技术领域。The invention relates to a method for concentrating coal bed gas, which belongs to the technical field of gas separation.
背景技术 Background technique
随着人们对煤矿安全、环境保护意识的提高，近年来国内外十分重视煤层气的开发利用。煤层气的有效成分是CH4，CH4是一种高效洁净的能源和化工原料，但同时也是一种温室效应气体。我国是煤炭资源大国，煤层气储量丰富，为35万亿立方米，居世界第三位。埋深2000米以内的煤层气资源量达31.46万亿立方米，其中埋深1500米以内的约占总资源量的60％。而目前我国每年因采煤排放的煤层气在130亿立方米以上，占世界煤层气排放总量的1/3，居世界第一。在当前我国天然气能源不足的情况下，人们在广泛注重常规天然气开发的同时，不断地将目光投向非常规天然气——煤层气的开发与利用。如果能有效利用这些煤层气资源，对改善和优化能源结构、保障煤矿安全生产、减少大气污染有重要的意义。With the improvement of people's awareness of coal mine safety and environmental protection, the development and utilization of coalbed methane have been attached great importance both at home and abroad in recent years. The effective component of coalbed methane is CH 4 , which is an efficient and clean energy and chemical raw material, but it is also a greenhouse gas. my country is a country with a large amount of coal resources, and its reserves of coalbed methane are 35 trillion cubic meters, ranking third in the world. The coalbed methane resources buried within 2,000 meters reach 31.46 trillion cubic meters, of which 60% of the total resources are buried within 1,500 meters. At present, my country's annual coal-bed methane emissions due to coal mining are more than 13 billion cubic meters, accounting for 1/3 of the world's total coal-bed methane emissions, ranking first in the world. In the current situation of insufficient natural gas energy in my country, people are constantly focusing on the development and utilization of unconventional natural gas—coal bed methane, while extensively focusing on the development of conventional natural gas. If these coalbed methane resources can be effectively utilized, it will be of great significance to improving and optimizing the energy structure, ensuring safe production in coal mines, and reducing air pollution.
煤层气作为一种高效清洁能源，主要成分是CH4，其次是N2和O2，另外还有少量或微量的烃类气体以及CO2、H2、He、H2S等，热均值为35800kJ/m3(相当于1.22kg标准煤)，燃烧过程中基本无烟尘。CH4的热值为33500～33700kJ/m3，按热值计算，大致1000m3CH4相当于1t标准煤。目前我国的煤层气利用基本上是CH4浓度在35％以上的用于民用，低浓度CH4则直接排放到大气当中。CH4是一种温室气体，会对环境造成了严重的破坏，它的温室效应比CO2要大20倍，将其排入大气层，不仅因为会温室效应引起气候异常，还会消耗大气平流层中的臭氧，对臭氧层破坏能力是CO2的7倍。As a high-efficiency and clean energy, coalbed methane is mainly composed of CH 4 , followed by N 2 and O 2 , and there are also a small or trace amount of hydrocarbon gas and CO 2 , H 2 , He, H 2 S, etc. The average thermal value is 35800kJ/m 3 (equivalent to 1.22kg standard coal), basically no smoke during combustion. The calorific value of CH 4 is 33,500-33,700 kJ/m 3 . According to the calorific value, roughly 1,000 m 3 CH 4 is equivalent to 1 ton of standard coal. At present, China's coalbed methane is basically used for civilian use with a CH 4 concentration above 35%, while low-concentration CH 4 is directly discharged into the atmosphere. CH 4 is a greenhouse gas that will cause serious damage to the environment. Its greenhouse effect is 20 times greater than that of CO 2 . Ejecting it into the atmosphere will not only cause climate anomalies due to the greenhouse effect, but also consume the atmospheric stratosphere Ozone in the atmosphere is 7 times more powerful than CO 2 in destroying the ozone layer.
煤层气中除空气外杂质含量相对较少，经过脱硫、干燥等预处理的煤层气成份为CH4、N2及O2，以CH4/空气或CH4/N2表示，也就是说，预净化后煤层气的分离实质上是CH4与N2之间的分离。The content of impurities in coalbed methane is relatively small except for air, and the components of coalbed methane after pretreatment such as desulfurization and drying are CH 4 , N 2 and O 2 , expressed as CH 4 /air or CH 4 /N 2 , that is, The separation of CBM after pre-purification is essentially the separation between CH4 and N2 .
目前，国内外主要的浓缩煤层气技术有：At present, the main concentrated coalbed methane technologies at home and abroad include:
(1)膜分离：膜分离技术是以膜两侧气体的分压差为推动力，通过溶解、扩散、脱附等步骤产生组分间传递速率的差异来实现分离。膜分离用于煤层气中CH4/N2分离有设备简单、过程无相态变化、占地少、可连续运行等优点；但膜分离过程中产品气的损失不可避免，给煤层气生产带来一定的安全隐患；另外膜分离的效果对制膜技术依赖性强，技术上还有较大的完善空间。(1) Membrane separation: Membrane separation technology uses the partial pressure difference of the gas on both sides of the membrane as the driving force, and achieves separation through the steps of dissolution, diffusion, and desorption to generate differences in the transfer rates between components. Membrane separation for CH 4 /N 2 separation in coalbed methane has the advantages of simple equipment, no phase change in the process, less land occupation, and continuous operation; In addition, the effect of membrane separation is highly dependent on membrane production technology, and there is still a lot of room for improvement in technology.
(2)低温精馏技术：低温精馏技术的分离原理是利用N2与CH4的沸点差实现二者的分离。低温精馏法分离N2和CH4混合气技术成熟、产品气浓度高、目的产物收率高，但装置复杂，设备投资大，能耗高，适用于处理量大的煤层气。(2) Cryogenic rectification technology: The separation principle of cryogenic rectification technology is to use the difference in boiling point of N 2 and CH 4 to separate them. Cryogenic rectification is a mature technology for separating N 2 and CH 4 mixed gas, with high product gas concentration and high yield of target product, but the device is complex, equipment investment is large, and energy consumption is high, so it is suitable for coalbed methane with a large amount of treatment.
(3)Mehra工艺：利用碳氢溶剂物理吸收CH4，实现N2和CH4混合物的分离。该工艺对同时回收天然气凝液和提浓含氮天然气有一定经济价值，但单独用来分离CH4和N2时，CH4在碳氢溶剂中溶解度低、需要吸收剂的量大，是否可行未见报道。(3) Mehra process: use hydrocarbon solvent to physically absorb CH 4 to realize the separation of N 2 and CH 4 mixture. This process has a certain economic value for recovering natural gas condensate and enriching nitrogen-containing natural gas at the same time, but when it is used alone to separate CH 4 and N 2 , CH 4 has low solubility in hydrocarbon solvents and requires a large amount of absorbent. Is it feasible? None reported.
(4)Bend研究机构采用金属基液体吸收剂去除N2：该机构制备了一种选择性化学吸收N2的金属有机络合物。当气体混合物通过溶有这种络合物的溶液时，N2与络合物反应生成新的物质而被选择性截留下来。该工艺理论可行，但溶液吸收再生速度慢，效率低，仅适合少量N2吸收，目前尚未进行工业现场试验。(4) The Bend Research Institute used metal-based liquid absorbents to remove N 2 : the institute prepared a metal-organic complex that selectively chemically absorbs N 2 . When the gas mixture passes through the solution in which the complex is dissolved, N2 reacts with the complex to form a new substance which is selectively trapped. The process is theoretically feasible, but the solution absorption and regeneration speed is slow and the efficiency is low. It is only suitable for a small amount of N2 absorption, and no industrial field test has been carried out yet.
(5)变压吸附(PSA)：变压吸附是利用吸附剂对气体混合物各组分的吸附强度、在吸附剂颗粒内外扩散的动力学效应或吸附剂颗粒内微孔对各组分分子位阻效应的不同，以压力的循环变化为分离推动力，使一种或多种组分得以浓缩或纯化。PSA是目前实现工业化气体吸附分离的主要技术之一，已广泛应用于石油化工、钢铁、冶金等领域。变压吸附应用于煤层气中CH4和N2分离，具有能耗低、操作灵活方便、常温下连续运行等优点。但是，大多数工业化的、应用最为成功的变压吸附过程都是弱吸附组分为产品，强吸附组分因其浓度低而没有得到广泛应用。目前工业化变压吸附分离CH4/N2混合体系，主要集中在以平衡为基础的分离技术上，产品气CH4为解吸气。这种变压吸附工艺的主要缺点就是：CH4为解吸气，解吸气中含有一定量的轻吸附组分，导致产品气的纯度不够高；而且一次吸附达到的提浓效果并不理想。根据CH4和N2物理性质的不同，CH4和N2分子存在较小、但可操作的动力学直径差异：CH4动力学直径为0.382nm，N2动力学直径为0.368nm。如果以动力学为基础进行分离，则CH4/N2混合体系分离过程中N2在吸附剂上的扩散较快，为易吸附组分。基于上述物性差别，研究人员对以动力学为基础的分离技术做了大量基础研究，但是对于解吸气为N2，出口气为产品气CH4的变压吸附工艺，尚未见报道。(5) Pressure swing adsorption (PSA): Pressure swing adsorption is the use of the adsorption strength of the adsorbent for each component of the gas mixture, the kinetic effect of diffusion inside and outside the adsorbent particles, or the molecular position of each component by the micropores in the adsorbent particles. The difference in the resistance effect, the cyclical change of the pressure is used as the driving force for separation, so that one or more components can be concentrated or purified. PSA is currently one of the main technologies for industrialized gas adsorption and separation, and has been widely used in petrochemical, steel, metallurgy and other fields. Pressure swing adsorption is applied to the separation of CH 4 and N 2 in coalbed methane, and has the advantages of low energy consumption, flexible and convenient operation, and continuous operation at room temperature. However, most industrialized and most successfully applied pressure swing adsorption processes use weakly adsorbed components as products, and strongly adsorbed components have not been widely used because of their low concentrations. At present, the industrial pressure swing adsorption separation CH 4 /N 2 mixed system mainly focuses on the separation technology based on equilibrium, and the product gas CH 4 is desorbed gas. The main disadvantage of this pressure swing adsorption process is: CH4 is the desorption gas, which contains a certain amount of light adsorption components, resulting in insufficient purity of the product gas; and the enrichment effect achieved by one-time adsorption is not ideal. . Depending on the physical properties of CH4 and N2 , there is a small, but manageable, kinetic diameter difference between CH4 and N2 molecules: 0.382 nm for CH4 and 0.368 nm for N2 . If the separation is based on kinetics, the diffusion of N 2 on the adsorbent is relatively fast during the separation process of the CH 4 /N 2 mixed system, and it is the easily adsorbed component. Based on the above differences in physical properties, researchers have done a lot of basic research on kinetic-based separation technology, but there is no report on the pressure swing adsorption process in which the desorbed gas is N 2 and the outlet gas is product gas CH 4 .
发明内容 Contents of the invention
本发明的目的在于提供一种煤层气直接富集甲烷的变压吸附工艺，采用变压吸附技术，通过加压吸附，N2在固定吸附床中的吸附剂上吸附，达到在出口直接富集CH4的目的；真空或降压解吸，达到吸附剂再生及循环使用的目的。本工艺可实现煤层气的有效开发利用和环境保护。The purpose of the present invention is to provide a pressure swing adsorption process for directly enriching methane from coalbed methane, using pressure swing adsorption technology, through pressure adsorption, N2 is adsorbed on the adsorbent in the fixed adsorption bed to achieve direct enrichment at the outlet The purpose of CH 4 ; vacuum or decompression desorption, to achieve the purpose of adsorbent regeneration and recycling. The process can realize effective development and utilization of coal bed gas and environmental protection.
进一步，本发明可通过以下技术方案实现：Further, the present invention can be realized through the following technical solutions:
本发明一个操作周期包括以下步骤(以第一吸附塔为例说明)：An operating cycle of the present invention comprises the following steps (taking the first adsorption tower as an example):
第一步吸附：打开原料气输出阀及产品气罐输入阀，原料气从第一吸附塔入口端进入进行吸附，产品气从第一吸附塔出口端流出进入产品气罐。The first step of adsorption: open the raw material gas output valve and the product gas tank input valve, the raw material gas enters from the inlet of the first adsorption tower for adsorption, and the product gas flows out from the outlet of the first adsorption tower into the product gas tank.
所述步骤中参数条件：温度控制在-80～120℃范围内，压力控制在0.1～1MPa范围内。Parameter conditions in the step: the temperature is controlled within the range of -80-120° C., and the pressure is controlled within the range of 0.1-1 MPa.
第二步均压：用事先抽好真空的吸附塔对第一吸附塔进行压力均衡。均压的目的是回收机械能，增加产品气体的回收率。The second step of pressure equalization: Use the adsorption tower that has been evacuated in advance to equalize the pressure of the first adsorption tower. The purpose of pressure equalization is to recover mechanical energy and increase the recovery rate of product gas.
第三步逆向减压：均压完成之后，对第一吸附塔进行逆向减压至大气压，然后逆向抽真空，使塔中吸附剂再生。The third step is reverse decompression: After the pressure equalization is completed, the first adsorption tower is reversely decompressed to atmospheric pressure, and then reversely evacuated to regenerate the adsorbent in the tower.
所述步骤中参数条件：真空度为0.1-0MPa。抽真空温度可控制在80-150℃，高温有利于解吸。Parameter conditions in the steps: the degree of vacuum is 0.1-0 MPa. The vacuum temperature can be controlled at 80-150°C, and high temperature is conducive to desorption.
第四步充压：第一吸附塔抽真空完成时，用此时完成吸附的塔对第一吸附塔进行第一次充压(此过程也可看成是一次均压过程)，再用产品气对第一吸附塔完成最终充压至操作压力，至此完成一个周期的操作。The fourth step of pressurization: when the vacuuming of the first adsorption tower is completed, use the tower that has completed the adsorption at this time to pressurize the first adsorption tower for the first time (this process can also be regarded as a pressure equalization process), and then use the product The gas is finally charged to the operating pressure for the first adsorption tower, and a cycle of operation has been completed so far.
所述步骤中参数条件：温度控制在-80～120℃范围内，压力控制在0.1～1MPa范围内；Parameter conditions in the steps: the temperature is controlled within the range of -80 to 120°C, and the pressure is controlled within the range of 0.1 to 1MPa;
本发明实现连续生产是通过以下方法实现的：The present invention realizes continuous production and is realized by the following methods:
第一吸附塔吸附的同时第四吸附塔进行抽真空，第二吸附塔和第三吸附塔进行快速均压。当第一吸附塔吸附完成，第四吸附塔停止抽真空。第四吸附塔对第一吸附塔均压，均压后第一吸附塔进入逆向减压抽真空阶段，此时对第三吸附塔进行产品气快速充压，进入吸附阶段，吸附完成之后，第三吸附塔对此时抽好真空的第一吸附塔进行第一次充压(可看作是一次均压)，然后改用产品气对第一吸附塔进行终充压，则第一吸附塔再一次进入吸附阶段。总之，四塔中保持一塔吸附，一塔抽真空，两塔均压，实现连续生产。While the first adsorption tower is adsorbing, the fourth adsorption tower is evacuated, and the second adsorption tower and the third adsorption tower are performing rapid pressure equalization. When the adsorption of the first adsorption tower is completed, the fourth adsorption tower stops vacuuming. The fourth adsorption tower equalizes the pressure on the first adsorption tower. After the pressure equalization, the first adsorption tower enters the reverse decompression and vacuuming stage. At this time, the third adsorption tower is quickly charged with product gas to enter the adsorption stage. After the adsorption is completed, the second adsorption tower The third adsorption tower pressurizes the first adsorption tower that has been evacuated at this time (it can be regarded as a pressure equalization), and then uses the product gas to carry out the final pressurization of the first adsorption tower, then the first adsorption tower Enter the adsorption stage again. In short, among the four towers, one tower is maintained for adsorption, the other tower is vacuumed, and the two towers are equalized to achieve continuous production.
所述的吸附剂为孔口改性的4A、5A沸石分子筛及炭分子筛。The adsorbent is 4A and 5A zeolite molecular sieves and carbon molecular sieves with modified pores.
所述经过孔口改性的4A、5A沸石分子筛及炭分子筛含有大部分孔径为0.3nm-0.5nm的微孔。The 4A and 5A zeolite molecular sieves and the carbon molecular sieves with modified pores contain most of the micropores with a pore diameter of 0.3nm-0.5nm.
本发明克服了现有技术中变压吸附工艺的缺点，采用经孔口修饰的吸附剂，选择对应的操作条件，研究了以动力学为基础的分离工艺，实现了在吸附剂上富集易吸附组分N2，出口直接富集产品气CH4的连续化生产。N2可以采用抽真空解吸，吸附剂再生比较容易，产品气的回收率也得到了提高，而且采用多塔变压吸附实现了连续化生产，CH4的纯度可达95％-99.9％，能够作为一种高效、清洁的能源和化工原料使用，还可以通入天然气管道。本发明对煤层气资源综合利用、改善能源结构、降低煤矿区事故的发生率以及环境保护具有重要的经济和环境意义。The invention overcomes the shortcomings of the pressure swing adsorption process in the prior art, adopts the adsorbent modified by the orifice, selects the corresponding operating conditions, studies the separation process based on kinetics, and realizes easy enrichment on the adsorbent. Continuous production of adsorbing component N 2 and directly enriching product gas CH 4 at the outlet. N2 can be desorbed by vacuum, the regeneration of the adsorbent is relatively easy, the recovery rate of the product gas has also been improved, and the continuous production has been realized by using multi-tower pressure swing adsorption, the purity of CH4 can reach 95%-99.9%, which can As an efficient and clean energy and chemical raw material, it can also be connected to natural gas pipelines. The invention has important economic and environmental significance for comprehensive utilization of coal bed gas resources, improvement of energy structure, reduction of accident rate in coal mining areas and environmental protection.
附图说明 Description of drawings
图1为实施案例1、实施案例2的工艺流程图。图中C1-第一吸附塔，C2-第二吸附塔，C3-第三吸附塔，C4-第四吸附塔，5-产品气罐，6-真空泵。Fig. 1 is the process flow diagram of implementation case 1 and implementation case 2. In the figure, C1-first adsorption tower, C2-second adsorption tower, C3-third adsorption tower, C4-fourth adsorption tower, 5-product gas tank, 6-vacuum pump.
图2为实施案例4CH4/N2混合体系的穿透曲线图。其中，CH4％∶N2％＝55∶45。Fig. 2 is the breakthrough curve of the CH 4 /N 2 mixed system of Example 4. Among them, CH 4 %:N 2 %=55:45.
具体实施方式 Detailed ways
本发明一个操作周期包括以下步骤(以第一吸附塔C1为例说明，以其他吸附塔为例说明是一样的，因为本四塔装置属于循环使用)：An operating cycle of the present invention comprises the following steps (taking the first adsorption tower C1 as an example, and taking other adsorption towers as an example to illustrate that it is the same, because the four tower devices belong to recycling):
第一步吸附：打开原料气输出阀及产品气罐5输入阀，原料气从第一吸附塔C1入口端进入进行吸附，产品气从第一吸附塔C1出口端流出进入产品气罐5。The first step of adsorption: open the raw material gas output valve and the
所述步骤中参数条件：温度控制在-80～120℃范围内，压力控制在0.1～1MPa范围内。Parameter conditions in the step: the temperature is controlled within the range of -80-120° C., and the pressure is controlled within the range of 0.1-1 MPa.
第二步均压：用事先抽好真空的吸附塔C2(第一吸附塔C1处于吸附状态时，其他几个塔是一个处于抽真空状态，两个快速均压即可，没有严格的塔工作状况的界定，因为被操作为循环过程，所以这里其实可以是在第一吸附塔吸C1吸附过程中第二吸附塔C2或者第三吸附塔C3或者第四吸附塔C4处于抽真空状态，抽真空完毕后对吸附完毕的吸附塔进行充压)对第一吸附塔C1进行压力均衡。均压的目的是回收机械能，增加产品气体的回收率。The second step of pressure equalization: use the adsorption tower C2 that has been evacuated in advance (when the first adsorption tower C1 is in the adsorption state, the other several towers are in a vacuum state, and two quick pressure equalizations are enough, there is no strict tower work The definition of the state, because it is operated as a cyclic process, so here can actually be that the second adsorption tower C2 or the third adsorption tower C3 or the fourth adsorption tower C4 is in a vacuum state during the adsorption process of the first adsorption tower C1. After completion, pressurize the adsorption tower that has been adsorbed) and perform pressure equalization on the first adsorption tower C1. The purpose of pressure equalization is to recover mechanical energy and increase the recovery rate of product gas.
第三步逆向减压：均压完成之后，对第一吸附塔C1进行逆向减压至大气压，然后逆向抽真空，使塔中吸附剂再生。The third step is reverse decompression: After the pressure equalization is completed, the first adsorption tower C1 is reversely decompressed to atmospheric pressure, and then reversely evacuated to regenerate the adsorbent in the tower.
所述步骤中参数条件：真空度为0.1～0MPa。抽真空温度可控制在80～150℃，高温有利于解吸。Parameter conditions in the steps: the degree of vacuum is 0.1-0 MPa. The vacuum temperature can be controlled at 80-150°C, and high temperature is conducive to desorption.
第四步充压：第一吸附塔C1抽真空完成时，用此时完成吸附的塔对第一吸附塔C1进行第一次充压(此过程也可看成是一次均压过程)，再用产品气对第一吸附塔C1完成最终充压至操作压力，至此完成一个周期的操作。The fourth step of pressurization: when the vacuuming of the first adsorption tower C1 is completed, use the tower that has completed the adsorption at this time to pressurize the first adsorption tower C1 for the first time (this process can also be regarded as a pressure equalization process), and then Use the product gas to complete the final pressurization of the first adsorption tower C1 to the operating pressure, and thus complete a cycle of operation.
所述步骤中参数条件：温度控制在-80～120℃范围内，压力控制在0.1～1MPa范围内。Parameter conditions in the step: the temperature is controlled within the range of -80-120° C., and the pressure is controlled within the range of 0.1-1 MPa.
本发明实现连续生产是通过以下方法实现的：The present invention realizes continuous production and is realized by the following methods:
第一吸附塔C1吸附的同时第四吸附塔C4进行抽真空，第二吸附塔C2和第三吸附塔C3进行快速均压。当第一吸附塔C1吸附完成，第四吸附塔C4停止抽真空。第四吸附塔C4对第一吸附塔C1均压，均压后第一吸附塔C1进入逆向减压抽真空阶段，此时对第三吸附塔C3进行产品气快速充压，进入吸附阶段，吸附完成之后，第三吸附塔C3对此时抽好真空的第一吸附塔C1进行第一次充压(可看作是一次均压)，然后改用产品气对第一吸附塔C1进行终充压，则第一吸附塔C1再一次进入吸附阶段。总之，四塔中保持一塔吸附，一塔抽真空，两塔均压，实现连续生产。While the first adsorption tower C1 is adsorbing, the fourth adsorption tower C4 is evacuated, and the second adsorption tower C2 and the third adsorption tower C3 are performing rapid pressure equalization. When the adsorption of the first adsorption tower C1 is completed, the fourth adsorption tower C4 stops vacuuming. The fourth adsorption tower C4 equalizes the pressure on the first adsorption tower C1. After the pressure equalization, the first adsorption tower C1 enters the reverse decompression and vacuuming stage. At this time, the third adsorption tower C3 is quickly charged with product gas and enters the adsorption stage. After the completion, the third adsorption tower C3 carries out the first pressurization of the first adsorption tower C1 which has been evacuated at this time (it can be regarded as a pressure equalization), and then uses the product gas to finally charge the first adsorption tower C1 pressure, the first adsorption tower C1 enters the adsorption stage again. In short, among the four towers, one tower is maintained for adsorption, the other tower is vacuumed, and the two towers are equalized to achieve continuous production.
抽真空都是通过真空泵6来实现的。Vacuumizing is all realized by
实例1：CH4/N2混合体系提浓，其中，温度为20℃，压力为0.5MPa，流速为0.32cm/s，CH4％∶N2％＝55∶45。Example 1: Concentration of a CH 4 /N 2 mixed system, wherein the temperature is 20° C., the pressure is 0.5 MPa, the flow rate is 0.32 cm/s, and CH 4 %:N 2 %=55:45.
具体方法为：首先将系统压力和温度稳定至设定值，原料气稳定进入第一吸附塔C1进行吸附，吸附同时第二吸附塔C2与第三吸附塔C3进行均压，第四吸附塔C4抽真空。吸附与解吸时间相当，当第一吸附塔C1中吸附完成时，第四吸附塔C4抽真空停止。第四吸附塔C4对第一吸附塔C1均压，均压后第一吸附塔C1进入逆向减压抽真空阶段，此时对第三吸附塔C3进行产品气快速充压，进入吸附阶段，吸附完成之后，第三吸附塔C3对此时抽好真空的第一吸附塔C1进行第一次充压(可看作是一次均压)，然后改用产品气对第一吸附塔C1进行终充压，则第一吸附塔C1再一次进入吸附阶段。如此循环操作，最终CH4的浓度可以达到99％以上。时序控制为：吸附180秒，均压10秒，充压10秒，解吸180秒。The specific method is: first stabilize the system pressure and temperature to the set value, the raw material gas stably enters the first adsorption tower C1 for adsorption, and at the same time, the second adsorption tower C2 and the third adsorption tower C3 perform pressure equalization, and the fourth adsorption tower C4 Vacuum. The time of adsorption and desorption is equivalent, when the adsorption in the first adsorption tower C1 is completed, the vacuuming of the fourth adsorption tower C4 stops. The fourth adsorption tower C4 equalizes the pressure on the first adsorption tower C1. After the pressure equalization, the first adsorption tower C1 enters the reverse decompression and vacuuming stage. At this time, the third adsorption tower C3 is quickly charged with product gas and enters the adsorption stage. After the completion, the third adsorption tower C3 carries out the first pressurization of the first adsorption tower C1 which has been evacuated at this time (it can be regarded as a pressure equalization), and then uses the product gas to finally charge the first adsorption tower C1 pressure, the first adsorption tower C1 enters the adsorption stage again. With such circular operation, the final concentration of CH 4 can reach more than 99%. The timing control is: adsorption for 180 seconds, pressure equalization for 10 seconds, pressure charging for 10 seconds, and desorption for 180 seconds.
实例2：CH4/N2混合体系提浓，其中，温度为20℃，压力为0.5MPa，流速为0.40cm/s，CH4％∶N2％＝30∶70Example 2: Concentration of CH 4 /N 2 mixed system, wherein the temperature is 20°C, the pressure is 0.5 MPa, the flow rate is 0.40 cm/s, CH 4 %:N 2 %=30:70
具体方法为：首先将系统压力和温度稳定至设定值，产品气对其充压，稳定后改用原料气稳定进入吸附塔进行吸附，吸附同时第二吸附塔C2与第三吸附塔C3进行均压，第四吸附塔C4抽真空。吸附与解吸时间相当，当第一吸附塔C1中吸附完成时，第四吸附塔C4抽真空停止。第四吸附塔C4对第一吸附塔C1均压，均压后第一吸附塔C1进入逆向减压抽真空阶段，此时对第三吸附塔C3进行产品气快速充压，进入吸附阶段，吸附完成之后，第三吸附塔C3对此时抽好真空的第一吸附塔C1进行第一次充压(可看作是一次均压)，然后改用产品气对第一吸附塔C1进行终充压，则第一吸附塔C1再一次进入吸附阶段。如此循环操作，最终CH4浓度要求在99％以上时，单程收率达64.8％。时序控制为：吸附120秒，均压10秒，充压10秒，解吸120秒。The specific method is: first stabilize the system pressure and temperature to the set value, pressurize it with the product gas, and then use the raw material gas to stably enter the adsorption tower for adsorption. At the same time, the second adsorption tower C2 and the third adsorption tower C3 carry out adsorption. Pressure equalization, the fourth adsorption tower C4 is evacuated. The time of adsorption and desorption is equivalent, when the adsorption in the first adsorption tower C1 is completed, the vacuuming of the fourth adsorption tower C4 stops. The fourth adsorption tower C4 equalizes the pressure on the first adsorption tower C1. After the pressure equalization, the first adsorption tower C1 enters the reverse decompression and vacuuming stage. At this time, the third adsorption tower C3 is quickly charged with product gas and enters the adsorption stage. After the completion, the third adsorption tower C3 carries out the first pressurization of the first adsorption tower C1 which has been evacuated at this time (it can be regarded as a pressure equalization), and then uses the product gas to finally charge the first adsorption tower C1 pressure, the first adsorption tower C1 enters the adsorption stage again. Such circular operation, when the final CH concentration is required to be above 99%, the single pass yield can reach 64.8%. The timing control is: adsorption for 120 seconds, pressure equalization for 10 seconds, pressure charging for 10 seconds, and desorption for 120 seconds.
实例3：CH4/N2混合体系提浓，其中，温度为0℃，压力为0.5MPa，流速为0.32cm/s，CH4％∶N2％＝20∶80。Example 3: Concentration of a CH 4 /N 2 mixed system, wherein the temperature is 0° C., the pressure is 0.5 MPa, the flow rate is 0.32 cm/s, and CH 4 %:N 2 %=20:80.
具体方法为：首先将系统压力和温度稳定至设定值，原料气稳定进入第一吸附塔C1进行吸附，吸附同时第二吸附塔C2与第三吸附塔C3进行均压，第四吸附塔C4抽真空。吸附与解吸时间相当，当第一吸附塔C1中吸附完成时，第四吸附塔C4抽真空停止。第四吸附塔C4对第一吸附塔C1均压，均压后第一吸附塔C1进入逆向减压抽真空阶段，此时对第三吸附塔C3进行产品气快速充压，进入吸附阶段，吸附完成之后，第三吸附塔C3对此时抽好真空的第一吸附塔C1进行第一次充压(可看作是一次均压)，然后改用产品气对第一吸附塔C1进行终充压，则第一吸附塔C1再一次进入吸附阶段。如此循环操作，最终CH4的浓度可以达到99％以上。时序控制为：吸附150秒，均压10秒，充压10秒，解吸150秒。The specific method is: first stabilize the system pressure and temperature to the set value, the raw material gas stably enters the first adsorption tower C1 for adsorption, and at the same time, the second adsorption tower C2 and the third adsorption tower C3 perform pressure equalization, and the fourth adsorption tower C4 Vacuum. The time of adsorption and desorption is equivalent, when the adsorption in the first adsorption tower C1 is completed, the vacuuming of the fourth adsorption tower C4 stops. The fourth adsorption tower C4 equalizes the pressure on the first adsorption tower C1. After the pressure equalization, the first adsorption tower C1 enters the reverse decompression and vacuuming stage. At this time, the third adsorption tower C3 is quickly charged with product gas and enters the adsorption stage. After the completion, the third adsorption tower C3 carries out the first pressurization of the first adsorption tower C1 which has been evacuated at this time (it can be regarded as a pressure equalization), and then uses the product gas to finally charge the first adsorption tower C1 pressure, the first adsorption tower C1 enters the adsorption stage again. With such circular operation, the final concentration of CH 4 can reach more than 99%. The timing control is: adsorption for 150 seconds, pressure equalization for 10 seconds, pressure charging for 10 seconds, and desorption for 150 seconds.
实例4：CH4/N2混合体系提浓，其中，温度为60℃，压力为0.5MPa，流速为0.40cm/s，CH4％∶N2％＝55∶45。Example 4: Concentration of CH 4 /N 2 mixed system, wherein the temperature is 60° C., the pressure is 0.5 MPa, the flow rate is 0.40 cm/s, CH 4 %:N 2 %=55:45.
具体方法为：首先将系统压力和温度稳定至设定值，原料气稳定进入第一吸附塔C1进行吸附，吸附同时第二吸附塔C2与第三吸附塔C3进行均压，第四吸附塔C4抽真空。吸附与解吸时间相当，当第一吸附塔C1中吸附完成时，第四吸附塔C4抽真空停止。第四吸附塔C4对第一吸附塔C1均压，均压后第一吸附塔C1进入逆向减压抽真空阶段，此时对第三吸附塔C3进行产品气快速充压，进入吸附阶段，吸附完成之后，第三吸附塔C3对此时抽好真空的第一吸附塔C1进行第一次充压(可看作是一次均压)，然后改用产品气对第一吸附塔C1进行终充压，则第一吸附塔C1再一次进入吸附阶段。如此循环操作，最终CH4的浓度要求在99％以上时，单程收率达75.6％，浓度要求在95％以上时，单程收率达67.7％。时序控制为：吸附120秒，均压10秒，充压10秒，解吸120秒。The specific method is: first stabilize the system pressure and temperature to the set value, the raw material gas stably enters the first adsorption tower C1 for adsorption, and at the same time, the second adsorption tower C2 and the third adsorption tower C3 perform pressure equalization, and the fourth adsorption tower C4 Vacuum. The time of adsorption and desorption is equivalent, when the adsorption in the first adsorption tower C1 is completed, the vacuuming of the fourth adsorption tower C4 stops. The fourth adsorption tower C4 equalizes the pressure on the first adsorption tower C1. After the pressure equalization, the first adsorption tower C1 enters the reverse decompression and vacuuming stage. At this time, the third adsorption tower C3 is quickly charged with product gas and enters the adsorption stage. After the completion, the third adsorption tower C3 carries out the first pressurization of the first adsorption tower C1 which has been evacuated at this time (it can be regarded as a pressure equalization), and then uses the product gas to finally charge the first adsorption tower C1 pressure, the first adsorption tower C1 enters the adsorption stage again. Such cyclic operation, when the final concentration of CH4 is required to be above 99%, the single-pass yield can reach 75.6%, and when the concentration is required to be above 95%, the single-pass yield can reach 67.7%. The timing control is: adsorption for 120 seconds, pressure equalization for 10 seconds, pressure charging for 10 seconds, and desorption for 120 seconds.
上述的对实施例的描述是为便于该技术领域的普通技术人员能理解和应用本发明。熟悉本领域技术的人员显然可以容易地对这些实施例做出各种修改，并把在此说明的一般原理应用到其他实施例中而不必经过创造性的劳动。因此，本发明不限于这里的实施例，本领域技术人员根据本发明的揭示，对于本发明做出的改进和修改都应该在本发明的保护范围之内。The above description of the embodiments is for those of ordinary skill in the art to understand and apply the present invention. It is obvious that those skilled in the art can easily make various modifications to these embodiments, and apply the general principles described here to other embodiments without creative effort. Therefore, the present invention is not limited to the embodiments herein, and improvements and modifications made by those skilled in the art according to the disclosure of the present invention should fall within the protection scope of the present invention.
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| CN101935032A (en) * | 2010-09-03 | 2011-01-05 | 同济大学 | A kind of preparation method and application of carbon molecular sieve |
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