CN104229735A - Integrated hydrogen recovery device - Google Patents
Integrated hydrogen recovery device Download PDFInfo
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- CN104229735A CN104229735A CN201310250470.9A CN201310250470A CN104229735A CN 104229735 A CN104229735 A CN 104229735A CN 201310250470 A CN201310250470 A CN 201310250470A CN 104229735 A CN104229735 A CN 104229735A
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- hydrogen
- swing adsorption
- pressure swing
- film separating
- pressure
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- Hydrogen, Water And Hydrids (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention provides an integrated hydrogen recovery device, relates to the technical fields of petroleum and chemical industry, and particularly relates to an integrated hydrogen recovery device, which integrates a film separation technique and a pressure swing adsorption technique, connects a film separation system and a pressure swing adsorption system through a pipeline, and classifies according to the parameters such as pressure energy, hydrogen concentration and flow of each hydrogen-containing tail gas. According to the difference of recovery targets, the device arrangement comprises three schemes, namely a film separation system and the catalytic dry gas PSA system are parallel, the film separation system and the catalytic dry gas PSA system are connected in series, the film separation system and the catalytic dry gas PSA system are parallel, a catalytic absorption and stabilization system is added to the pressure swing adsorption system, grading recovery of hydrogen is achieved, and a hydrogen resource with high recovery rate and purity can be obtained, the combined process integrates the advantages of simple process and low investment cost of a film separation technology, and high purity of a hydrogen product produced by the pressure swing adsorption technique. Therefore, the integrated hydrogen recovery device has high social benefits, environment-friendly benefits and economic benefits.
Description
Technical field
The present invention relates to a kind of device of integrated form recover hydrogen, particularly relate to the device of the parameter recovery hydrogen such as a kind of pressure energy according to hydrogen containing tail gas, density of hydrogen, flow, belong to technical field of petrochemical industry.
Background technology
Oil is disposable Nonrenewable energy resources, and its reserves are fewer and feweri, makes crude oil heaviness, in poor quality, sulphur content, metal content in rising trend, causes the ratio of refinery's Sulfur-Containing Crude and heavy crude to increase year by year.In order to the challenge of the demand and environment protection two aspect of tackling high-quality oil product and industrial chemicals, Ge great refinery has generally set up coking and hydrocracking operation, and therefore hydrogen addition technology is the effective means of refinery deep processing.But the hydrogen source in refinery mainly contains two kinds, one is produced with oil etc., and cost is higher, and another kind utilizes new technology to reclaim hydrogen from various hydrogen containing tail gas.
Because the parameter such as concentration, pressure, flow of each hydrogen containing tail gas is different, the present invention is by membrane separation technique and pressure-variable adsorption (Pressure Swing Adsorption, be called for short PSA) technology combination, classification recover hydrogen from hydrogen containing tail gas, the rate of recovery and all higher hydrogen resources of purity can be obtained, and process integration combines the advantage that membrane separation technique technique is simple, investment cost is few and pressure swing adsorption hydrogen manufacturing product purity is high, there is higher social benefit, environmental benefit and economic benefit.
Summary of the invention
The object of the present invention is to provide a kind of device of integrated form recover hydrogen.
This device Integrated Films is separated the advantage with pressure swing adsorption, film separating system and pressure swing adsorption system are linked together by pipeline, according to the parameter such as pressure energy, density of hydrogen, flow of each stock hydrogen containing tail gas, it is classified, be divided into high-pressure high-concentration large discharge hydrogen containing tail gas, middle pressure higher concentration low discharge hydrogen containing tail gas, low pressure high density large discharge hydrogen containing tail gas, according to concrete recovery target, select optimal separation technique, the classification realizing hydrogen is reclaimed, and improves the rate of recovery and the purity of hydrogen.
Described high-pressure high-concentration large discharge hydrogen containing tail gas: such as gauge pressure is at more than 1Mpa, concentration more than 30% and flow at 150Nm
3/ more than h; Middle pressure higher concentration low discharge hydrogen containing tail gas: such as gauge pressure is between 0.7 ~ 1Mpa, concentration more than 30% and flow at 150Nm
3/ below h; Low pressure high density large discharge hydrogen containing tail gas: such as gauge pressure is at below 0.7Mpa, concentration more than 30% and flow at 150Nm
3/ more than h.
Described retrieving arrangement film separating system comprises tail-gas compressor, desulphurization system, film separating system and hydrogen gas compressor; Pressure swing adsorption system comprises catalysis drying gas PSA system, optionally increases optimization of FCCU absorption-stabilization as required; Connected by pipeline between each equipment and system of described retrieving arrangement.
The Plant arrangement scheme of described integrated form recover hydrogen is divided into following 3 kinds: the first is that film separating system and catalysis drying gas PSA system are arranged side by side; The second is film separating system and catalysis drying gas PSA Cascade System; The third is that film separating system and catalysis drying gas PSA system are arranged side by side, and increases optimization of FCCU absorption-stabilization in pressure swing adsorption system.
The invention has the beneficial effects as follows: project environment is profitable, new pollution can not be caused; Recover hydrogen from hydrogen containing tail gas, had both decreased the unnecessary waste of hydrogen resource, alleviated again the problem of a large amount of hydrogen source of enterprise demand; By membrane sepn and pressure swing adsorption integrated, under different pressure energies, density of hydrogen, flow, realize hydrogen classification reclaim, broken the development bottleneck of monotechnics.
Accompanying drawing explanation
Fig. 1 is apparatus of the present invention hydrogen recovery schema 1;
Fig. 2 is apparatus of the present invention hydrogen recovery schema 2;
Fig. 3 is apparatus of the present invention hydrogen recovery schema 3.
Accompanying drawing: press higher concentration low discharge hydrogen containing tail gas, 5-tail-gas compressor, 6-desulphurization system, 7-film separating system, 8-hydrogen gas compressor, 9-catalysis drying gas PSA system, 10-C in 1-hydrogen pipe network, 2-high-pressure high-concentration large discharge hydrogen containing tail gas, 3-low pressure high density large discharge hydrogen containing tail gas, 4-
3, C
4the hydrogen containing tail gas that content is lower, 11-C
3, C
4the hydrogen containing tail gas that content is higher, 12-optimization of FCCU absorption-stabilization.
Embodiment
Below in conjunction with accompanying drawing, the present invention is described further:
Its layout of a kind of device of integrated form recover hydrogen comprises following 3 schemes:
Scheme 1 as shown in Figure 1, is comprised a tail-gas compressor 5, hydrogen gas compressor 8, a set of desulphurization system 6, a set of film separating system 7 and a set of catalysis drying gas PSA system 9, is linked together between each system and device by pipeline.Be specially film separating system 7 arranged side by side with catalysis drying gas PSA system 9, after the hydrogen containing tail gas 3 of low pressure high density large discharge collects with the hydrogen containing tail gas 2 of high-pressure high-concentration large discharge and mixes after tail-gas compressor 5 pressurizes, be transported to desulphurization system 6 and carry out desulfurization, then enter film separating system 7 and carry out film recovery, now film separating system 7 is purified each hydrogenation tail gas, enters hydrogen pipe net 1 be used after making it directly to reach hydrogen product concentration by hydrogen gas compressor 8 after being pressurizeed; The hydrogen containing tail gas 4 of middle pressure higher concentration low discharge directly enters catalysis drying gas PSA system 9, has processed the rear hydrogen pipe network 1 that directly enters and has been used.Film separating system 7 product H
2purity 95.8%, H
2the rate of recovery 95.9%, H
2reclaim tolerance 5757Nm
3/ h.Owing to pressing the hydrogen containing tail gas 4 of higher concentration low discharge in catalysis drying gas PSA system 9 process, treatment scale is at 9000Nm
3about/h, H
2the rate of recovery about 80%, hydrogen purity 99.9%.
Scheme 2 as shown in Figure 2, is comprised a tail-gas compressor 5, a set of desulphurization system 6, a set of film separating system 7 and a set of catalysis drying gas PSA system 9, is linked together between each system and device by pipeline.Be specially film separating system 7 to connect with catalysis drying gas PSA system 9, enter desulphurization system 6 together with after low pressure high density large discharge hydrogen containing tail gas 3 collects mixing with high-pressure high-concentration large discharge hydrogen containing tail gas 2 and middle pressure higher concentration low discharge hydrogen containing tail gas 4 after tail-gas compressor 5 pressurizes and carry out desulfurization, enter film separating system 7 afterwards and hydrogen containing tail gas is purified to about 66%, now hydrogen containing tail gas flow is 10000Nm
3about/h, then enters catalysis drying gas PSA system 9 and continues to purify, enter hydrogen pipe net 1 and be used after purification.Film separating system 7 product H
2purity 66.4%, H
2the rate of recovery 85.9%.Hydrogen containing tail gas after catalysis drying gas PSA system 9 process purification, treatment scale is at 10000Nm
3about/h, H
2the rate of recovery about 80%, H
2purity 99.9%.
Scheme 3 as shown in Figure 3, is comprised a set of desulphurization system 6, a set of film separating system 7, hydrogen gas compressor 8, a set of optimization of FCCU absorption-stabilization 12 and a set of catalysis drying gas PSA system 9, is linked together between each system and device by pipeline.Be specially film separating system 7 arranged side by side with catalysis drying gas PSA system 9, and before catalysis drying gas PSA system 9, increase a set of optimization of FCCU absorption-stabilization 12, by C
3, C
4hydrogen containing tail gas 11 (the C that content is higher
3, C
4content > 30%) deliver to optimization of FCCU absorption-stabilization 12, become catalysis drying gas after removing liquefied gas, enter catalysis drying gas PSA system 9, processed laggard enter hydrogen pipe network 1 be used.And C
3, C
4hydrogen containing tail gas 10 (the C that content is less
3, C
4content < 30%) directly enter desulphurization system 6 desulfurization after enter film separating system 7, after hydrogen gas compressor 8 supercharging, enter hydrogen pipe net 1 afterwards and be used.Film separating system 7 product H
2purity 96.2%, H
2the rate of recovery 96.1%.Catalysis drying gas PSA system 9 treatment scale is at 11400Nm
3about/h, H
2the rate of recovery about 80%, H
2purity 99.9%.
Claims (3)
1. the device of an integrated form recover hydrogen, its Integrated Films is separated the advantage with pressure swing adsorption, film separating system and pressure swing adsorption system are linked together by pipeline, according to the parameter such as pressure energy, density of hydrogen, flow of each stock hydrogen containing tail gas, it is classified, be divided into high-pressure high-concentration large discharge hydrogen containing tail gas, middle pressure higher concentration low discharge hydrogen containing tail gas, low pressure high density large discharge hydrogen containing tail gas, according to concrete recovery target, select optimal separation technique, the classification realizing hydrogen is reclaimed, and improves the rate of recovery and the purity of hydrogen.
2. the device film separating system of integrated form recover hydrogen comprises tail-gas compressor, desulphurization system, film separating system and hydrogen gas compressor according to claim 1; Pressure swing adsorption system comprises catalysis drying gas PSA system, optionally increases optimization of FCCU absorption-stabilization as required; Connected by pipeline between each equipment and system of described retrieving arrangement.
3. the device of integrated form recover hydrogen according to claim 1, its arrangement is divided into following 3 kinds: the first is that film separating system and catalysis drying gas PSA system are arranged side by side; The second is film separating system and catalysis drying gas PSA Cascade System; The third is that film separating system and catalysis drying gas PSA system are arranged side by side, and increases optimization of FCCU absorption-stabilization in pressure swing adsorption system.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310250470.9A CN104229735A (en) | 2013-06-24 | 2013-06-24 | Integrated hydrogen recovery device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310250470.9A CN104229735A (en) | 2013-06-24 | 2013-06-24 | Integrated hydrogen recovery device |
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| Publication Number | Publication Date |
|---|---|
| CN104229735A true CN104229735A (en) | 2014-12-24 |
Family
ID=52218760
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310250470.9A Pending CN104229735A (en) | 2013-06-24 | 2013-06-24 | Integrated hydrogen recovery device |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104495752A (en) * | 2014-12-31 | 2015-04-08 | 中国石油天然气股份有限公司 | Method and system for treating refinery gas by combining membrane separation and pressure swing adsorption |
| CN105984844A (en) * | 2015-02-03 | 2016-10-05 | 上海华林工业气体有限公司 | Device and method for controlling feeding temperature of crude hydrogen in pressure swing adsorption bed |
| CN110234620A (en) * | 2017-01-30 | 2019-09-13 | 三菱化学株式会社 | The manufacturing method of high concentration alcohol |
| CN111111381A (en) * | 2020-01-15 | 2020-05-08 | 福州大学化肥催化剂国家工程研究中心 | Adsorption column and hydrogen-nitrogen separation system |
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| CN1903703A (en) * | 2006-08-04 | 2007-01-31 | 四川亚联高科技有限责任公司 | Technological method of purifying hydrogen of hydrogen enriched gas source |
| CN101525120A (en) * | 2009-04-16 | 2009-09-09 | 罗东晓 | Method for utilizing refinery tail gas and coke oven gas efficiently and rationally |
| CN202063710U (en) * | 2011-06-01 | 2011-12-07 | 大连欧科膜技术工程有限公司 | Device for recovering hydrogen from refinery gas |
| CN202148183U (en) * | 2011-07-08 | 2012-02-22 | 南京荣欣化工有限公司 | Gas separation purification device |
-
2013
- 2013-06-24 CN CN201310250470.9A patent/CN104229735A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1903703A (en) * | 2006-08-04 | 2007-01-31 | 四川亚联高科技有限责任公司 | Technological method of purifying hydrogen of hydrogen enriched gas source |
| CN101525120A (en) * | 2009-04-16 | 2009-09-09 | 罗东晓 | Method for utilizing refinery tail gas and coke oven gas efficiently and rationally |
| CN202063710U (en) * | 2011-06-01 | 2011-12-07 | 大连欧科膜技术工程有限公司 | Device for recovering hydrogen from refinery gas |
| CN202148183U (en) * | 2011-07-08 | 2012-02-22 | 南京荣欣化工有限公司 | Gas separation purification device |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104495752A (en) * | 2014-12-31 | 2015-04-08 | 中国石油天然气股份有限公司 | Method and system for treating refinery gas by combining membrane separation and pressure swing adsorption |
| CN105984844A (en) * | 2015-02-03 | 2016-10-05 | 上海华林工业气体有限公司 | Device and method for controlling feeding temperature of crude hydrogen in pressure swing adsorption bed |
| CN110234620A (en) * | 2017-01-30 | 2019-09-13 | 三菱化学株式会社 | The manufacturing method of high concentration alcohol |
| CN110234620B (en) * | 2017-01-30 | 2022-08-26 | 三菱化学株式会社 | Method for producing high-concentration alcohol |
| CN111111381A (en) * | 2020-01-15 | 2020-05-08 | 福州大学化肥催化剂国家工程研究中心 | Adsorption column and hydrogen-nitrogen separation system |
| CN111111381B (en) * | 2020-01-15 | 2023-12-22 | 福大紫金氢能科技股份有限公司 | Adsorption column and hydrogen-nitrogen separation system |
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Application publication date: 20141224 |