CN1202901C - Single-stage process flow for side scavengeing with partial raw gas at low-pressure end - Google Patents
Single-stage process flow for side scavengeing with partial raw gas at low-pressure end Download PDFInfo
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- CN1202901C CN1202901C CN 00110113 CN00110113A CN1202901C CN 1202901 C CN1202901 C CN 1202901C CN 00110113 CN00110113 CN 00110113 CN 00110113 A CN00110113 A CN 00110113A CN 1202901 C CN1202901 C CN 1202901C
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- 238000000034 method Methods 0.000 title claims abstract description 38
- 239000012528 membrane Substances 0.000 claims abstract description 42
- 239000012466 permeate Substances 0.000 claims abstract description 20
- 239000000047 product Substances 0.000 claims abstract description 14
- 238000010926 purge Methods 0.000 claims abstract description 10
- 239000002994 raw material Substances 0.000 claims abstract description 8
- 238000013461 design Methods 0.000 abstract description 10
- 239000007789 gas Substances 0.000 description 58
- 238000000926 separation method Methods 0.000 description 16
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 12
- 239000001257 hydrogen Substances 0.000 description 12
- 229910052739 hydrogen Inorganic materials 0.000 description 12
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 230000035699 permeability Effects 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 229910021529 ammonia Inorganic materials 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- 238000011160 research Methods 0.000 description 3
- 238000007872 degassing Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000012467 final product Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
一种部分原料气在低压侧吹扫单级流程，其特征在于：原料气分成两路，其中一路自膜组件的高压端进入，另一路自膜组件低压端进入吹扫渗透侧，产品气为低压侧渗透气。本发明在完成相同的设计要求时，所需的膜组件数量少于传统流程，同时操作上也更具灵活性。
A part of the raw material gas is purged on the low-pressure side of the single-stage process, which is characterized in that: the raw material gas is divided into two paths, one of which enters from the high-pressure end of the membrane module, and the other enters the purge permeate side from the low-pressure end of the membrane module, and the product gas is Permeate air on the low pressure side. When the present invention fulfills the same design requirement, the required number of membrane modules is less than that of the traditional process, and at the same time, the operation is more flexible.
Description
本发明涉及膜分离技术，特别提供了一种部分原料气在低压侧吹扫单级流程。The invention relates to membrane separation technology, and in particular provides a single-stage process for purging part of raw gas on the low-pressure side.
流程设计、优化方法和原则的研究，经历了理想分级理论，连续膜柱理论，逆流循环分级理论等一系列过程。目前随着膜组件分离性能的提高，一些简单的多级流程正受到越来越多研究者的重视。由于过去的膜组件分离性能较低，因此为了达到较高的分离要求，在流程设计时，如何充分发挥膜组件的分离性能成为了一个重要的设计思想。但是，在流程设计中膜组件分离性能的充分体现往往是以牺牲渗透性能为代价的。如一个简单的二级流程(该流程往往被用于产品气浓度要求较高的分离过程)，由于总的压力差等于各级膜组件的压力差之和，因此每一级膜组件的压力差减小了，该级的渗透量也减小了，从而导致膜组件的渗透性能在该流程中得不到充分发挥。Prassad在1992年US Pat5,102,432中提出了一个用空气制备极高纯度氮气的三级流程。在该流程中，通过调整三级膜组件的膜面积分配，氮气浓度可达到99％～99.999％。该流程通过增加压缩机或压缩机功耗来降低所需膜组件数量。Prassad还在1993年US Pat5,185,014中提出了一个用空气制备富氧气的二级流程，在该流程中，部分或全部原料空气由第二级渗透侧进入，第二级渗透气被引入第一级高压侧，产品气为第一级渗透气。由于第二级渗透气的氧浓度大于空气中的氧浓度，因此用第二级渗透气作为第一级的原料气可以提高产品气浓度。Xu在1993年US Pat5,282,969中提出了一个二级气体膜分离流程，该流程用于原料气中快气浓度较低时，快气提浓过程，富氧过程是其中的一个应用实例。该流程是利用第二级渗透侧低浓度气体吹扫第一级渗透侧，以降低第一级渗透侧浓度，提高膜两侧快气的传质推动力，从而达到增加第一级快气渗透量的目的。Xu还在1994年USPat5,306,427中提出了一个三级气体膜分离流程，该流程用于原料气中快气浓度较低时，快气提浓过程，富氧过程是其中的一个应用实例。该流程在流程中增加了一个慢气富集段，即提馏段，将非渗透气中的慢气浓度进一步提纯。通过该流程可以使慢气、快气在分离过程得到同时富集。目前，随着膜分离技术的发展，膜组件的分离性能有了很大的提高，在流程设计中，如何充分发挥膜组件的渗透性能已经成为重要的研究课题，有关这方面的研究报道还很少。充分发挥膜组件的渗透性能，在最经济的条件下实现设计要求，对工程设计具有重要的实际意义。The research on process design, optimization methods and principles has gone through a series of processes such as ideal classification theory, continuous membrane column theory, and countercurrent circulation classification theory. At present, with the improvement of the separation performance of membrane modules, some simple multi-stage processes are being paid more and more attention by researchers. Due to the low separation performance of membrane modules in the past, in order to achieve higher separation requirements, how to give full play to the separation performance of membrane modules has become an important design idea in process design. However, the full reflection of the separation performance of the membrane module in the process design is often at the expense of the permeability performance. For example, a simple two-stage process (this process is often used in the separation process with high product gas concentration requirements), since the total pressure difference is equal to the sum of the pressure differences of the membrane modules at all levels, the pressure difference of each membrane module If it is reduced, the permeation volume of this stage is also reduced, resulting in that the permeation performance of the membrane module cannot be fully utilized in this process. Prassad proposed in 1992 US Pat5,102,432 a three-stage process for preparing extremely high-purity nitrogen from air. In this process, by adjusting the membrane area distribution of the three-stage membrane module, the nitrogen concentration can reach 99% to 99.999%. This process reduces the number of membrane modules required by increasing the compressor or compressor power consumption. Prassad also proposed a secondary process for preparing oxygen-enriched oxygen from air in US Pat5,185,014 in 1993. In this process, part or all of the feed air enters from the second-stage permeate side, and the second-stage permeate gas is introduced into the first stage. On the high-pressure side of the first stage, the product gas is the permeate gas of the first stage. Since the oxygen concentration of the second-stage permeate gas is greater than that in the air, using the second-stage permeate gas as the raw material gas of the first stage can increase the product gas concentration. Xu proposed a two-stage gas membrane separation process in US Pat 5,282,969 in 1993. This process is used for the fast gas concentration process when the fast gas concentration in the feed gas is low. The oxygen enrichment process is an application example. The process is to use the low-concentration gas on the second-stage permeate side to purge the first-stage permeate side to reduce the concentration on the first-stage permeate side and increase the mass transfer driving force of the fast gas on both sides of the membrane, so as to increase the permeation of the first-stage fast gas Quantitative purpose. Xu also proposed a three-stage gas membrane separation process in USPat 5,306,427 in 1994. This process is used for the fast gas concentration process when the fast gas concentration in the feed gas is low. The oxygen enrichment process is an application example. In this process, a slow gas enrichment section, that is, a stripping section, is added to the process to further purify the slow gas concentration in the non-permeable gas. Through this process, slow gas and fast gas can be simultaneously enriched during the separation process. At present, with the development of membrane separation technology, the separation performance of membrane modules has been greatly improved. In process design, how to give full play to the permeability performance of membrane modules has become an important research topic. There are still few research reports on this aspect. few. It is of great practical significance for engineering design to give full play to the permeability of membrane modules and realize the design requirements under the most economical conditions.
本发明的目的在于提供一种部分原料气在低压侧吹扫单级流程，其在完成相同的设计要求时，所需的膜组件数量少于传统流程，同时操作上也更具灵活性。The purpose of the present invention is to provide a single-stage flow process with part of the feed gas being purged on the low pressure side. When the same design requirements are met, the number of membrane modules required is less than that of the traditional flow process, and the operation is also more flexible.
本发明提供了一种部分原料气在低压侧吹扫单级流程，其特征在于：原料气分成两路，其中一路自膜组件的高压端进入，另一路自膜组件低压端进入吹扫渗透侧，产品气为低压侧渗透气。The invention provides a single-stage process for partly purging raw material gas on the low-pressure side, which is characterized in that: the raw material gas is divided into two paths, one of which enters from the high-pressure end of the membrane module, and the other enters from the low-pressure end of the membrane module to purge the permeate side , the product gas is the permeate gas on the low pressure side.
本发明流程中高压侧与低压侧气体流向可以是并流或逆流或错流。In the process of the present invention, the gas flow direction of the high-pressure side and the low-pressure side can be co-current, counter-current or cross-flow.
由于原料气不是全部由膜组件内部通过，一部分原料气未经过膜而直接与渗透气混合，所以产品气的总流量增大了；同时原料气进入低压侧，降低了该侧气体的浓度，提高了膜两侧气体的传质推动力，增加了气体通过膜的流量，从而进一步增加了产品气总流量。当产品气流量一定时，所需膜组件数量减少膜了。Since the feed gas does not pass through the membrane module entirely, a part of the feed gas directly mixes with the permeate gas without passing through the membrane, so the total flow rate of the product gas increases; at the same time, the feed gas enters the low-pressure side, reducing the concentration of the gas on this side and improving The mass transfer driving force of the gas on both sides of the membrane is increased, and the flow rate of the gas passing through the membrane is increased, thereby further increasing the total flow rate of the product gas. When the product gas flow rate is constant, the number of membrane modules required is reduced.
本发明特别适用于膜组件分离系数较高，产品气为渗透气的分离过程，如：合成氨驰放气氢回收过程；膜法富氧过程等。The invention is especially suitable for the separation process in which the separation coefficient of the membrane module is relatively high and the product gas is the permeate gas, such as the hydrogen recovery process of the degassing of synthetic ammonia, the oxygen enrichment process of the membrane method, and the like.
下面通过实施例详述本发明。The present invention is described in detail below by way of examples.
附图1为部分原料气在低压侧吹扫单级流程。Accompanying drawing 1 is a single-stage flow process for purging part of the feed gas on the low pressure side.
附图2为传统合成氨驰放气氢回收单级流程。Accompanying drawing 2 is the single-stage flow process of traditional synthetic ammonia purge gas hydrogen recovery.
实施例Example
合成氨驰放气氢回收过程流程设计如图1所示，原料气分成两路，其中一路自膜组件的高压端进入，另一路自膜组件低压端进入吹扫渗透侧，产品气为低压侧渗透气，所需膜面积为95m2；所用膜组件氢渗透系数5.0×10-5cm3(STP)/cm2 s cmHg，分离系数50；采用原料气氢浓度0.6，原料气流量1000m3(STP)/hr，原料侧压力11MPa，渗透侧压力2MPa，所得最终产品气氢收率0.85，产品气氢浓度0.85。The flow design of the hydrogen recovery process for synthetic ammonia degassing is shown in Figure 1. The raw material gas is divided into two paths, one of which enters from the high-pressure end of the membrane module, and the other enters the purge and permeate side from the low-pressure end of the membrane module, and the product gas permeates from the low-pressure side. gas, the required membrane area is 95m 2 ; the hydrogen permeability coefficient of the membrane module used is 5.0×10 -5 cm 3 (STP)/cm 2 s cmHg, and the separation coefficient is 50; the hydrogen concentration of the raw gas is 0.6, and the flow rate of the raw gas is 1000m 3 (STP )/hr, the raw material side pressure is 11MPa, the permeate side pressure is 2MPa, the resulting final product gas hydrogen yield is 0.85, and the product gas hydrogen concentration is 0.85.
比较例comparative example
流程如图1所示的传统合成氨驰放气氢回收过程，所用膜组件同实施例，即膜组件氢渗透系数5.0×10-5cm3(STP)/cm2 s cmHg，分离系数50；采用同样的原料气和操作参数，即原料气氢浓度0.6，原料气流量1000m3(STP)/hr，原料侧压力11MPa，渗透侧压力2MPa，当最终产品同样与实施例相同时，即产品气氢收率0.85，产品气氢浓度0.85；所需膜面积为155m2，比实施例所需膜面积高很多。The process flow shown in Figure 1 is the traditional hydrogen recovery process for the exhaust gas of synthetic ammonia. The membrane module used is the same as that in the embodiment, that is, the hydrogen permeability coefficient of the membrane module is 5.0×10 -5 cm 3 (STP)/cm 2 s cmHg, and the separation coefficient is 50; The same feed gas and operating parameters, that is, feed gas hydrogen concentration 0.6, feed gas flow rate 1000m 3 (STP)/hr, feed side pressure 11MPa, permeate side pressure 2MPa, when the final product is also the same as the embodiment, that is, the product gas hydrogen The yield is 0.85, and the hydrogen concentration of the product gas is 0.85; the required membrane area is 155 m 2 , which is much higher than the required membrane area in the examples.
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| CN 00110113 CN1202901C (en) | 2000-02-16 | 2000-02-16 | Single-stage process flow for side scavengeing with partial raw gas at low-pressure end |
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| CN 00110113 CN1202901C (en) | 2000-02-16 | 2000-02-16 | Single-stage process flow for side scavengeing with partial raw gas at low-pressure end |
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| CN1308984A CN1308984A (en) | 2001-08-22 |
| CN1202901C true CN1202901C (en) | 2005-05-25 |
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Granted publication date: 20050525 Termination date: 20140216 |