CN101982403A - Hydrogen purification and transportation method - Google Patents
Hydrogen purification and transportation method Download PDFInfo
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- CN101982403A CN101982403A CN 201010508091 CN201010508091A CN101982403A CN 101982403 A CN101982403 A CN 101982403A CN 201010508091 CN201010508091 CN 201010508091 CN 201010508091 A CN201010508091 A CN 201010508091A CN 101982403 A CN101982403 A CN 101982403A
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Abstract
The invention relates to a hydrogen purification and transportation method which comprises the following steps: 1. a gas mixture containing water vapor and hydrogen from the upstream industrial production of sodium chlorate firstly enters a cooler, the gas mixture is cooled, the cooled synthetic gas enters a gas-liquid separator, the condensed water vapor is separated from the gas mixture, and the condensation water is discharged into a water seal; 2. the dewatered gas mixture obtained in step 1 enters an active carbon adsorption plant; and 3. the gas processed in step 2 is sent into a dry gas-holder to be stored, and the gas in the dry gas-holder is compressed by a compressor and then sent to the outside.
Description
Technical field
The present invention relates to a kind of industrial hydrogen production technical field, especially relate to a kind of purification and carrying method of production of sodium chlorate byproduct hydrogen.
Background technology
The development of China's hydrogen peroxide manufacture method, roughly experienced anthraquinone 3 developmental stage of the anthraquinone and palladium catalyst fixed bed hydrogenation technology of electrolytic process, nickel catalyzator stirring tank hydrogenation process according to the priority of time, the anthraquinone of palladium catalyst fixed bed hydrogenation technology is main production methods at present.Hydrogen dioxide solution production by anthraquinone process is to be carrier with 2-EAQ and tetrahydrochysene 2-EAQ, and heavy aromatics and trioctyl phosphate are mixed solvent, are mixed with working fluid.This working fluid and hydrogen together enter in the fixed bed that the palladium catalyst is housed, and carry out hydrogenation under certain pressure and temperature condition, obtain corresponding hydrogen anthraquinone solution (title hydride).Hydride carries out oxidation with air in oxidizing tower, the hydrogen anthraquinone in the hydride is reduced into original anthraquinone, generates hydrogen peroxide simultaneously.
The source of hydrogen mainly contains following several respects at present: water electrolysis method: the hydrogen purity that provides is higher, can obtain high-purity hydrogen by further purification, but investment is bigger, the energy consumption height, and hydrogen source cost is higher; From the process gas of Chemical Manufacture or process gas, purify and obtain hydrogen, in the nitrogen and hydrogen mixture and hydrocarbon steam conversion gas that decomposes such as catalytic cracking tail gas from the water-gas of chemical fertilizers production, petrochemical complex, ammonia, separate with purified gases with membrane sepn or pressure swing absorption process and to obtain hydrogen, general industrial scale is bigger, and the plant hydrogen of production is mainly used in industrial hydrogenation or compound probability.Adopt cheap hydrogen to make raw material, fully utilizing other industry byproduct hydrogen is to build the factor that the hydrogen peroxide manufacture line should be considered, press hydrogen source cost height, reasonably the hydrogen source selection is chlorine industry byproduct recover hydrogen, petrochemical by-product hydrogen, synthetic ammonia relief gas recover hydrogen and other Chemical Manufacture byproduct recover hydrogen successively.The hydrogen that the chlorine industry byproduct reclaims, have that impurity is many, purity is low, water content exceeds standard in the hydrogen, can be to causing the safe and continuous running period of work-ing life of the normal operation of hydrogen gas compressor, process for prepairng hydrogen peroxide by anthraquinone fixed bed catalyst and device etc. tremendous influence, thereby need impurity in the recover hydrogen and moisture are removed, to reach the requirement that is suitable for hydrogen peroxide manufacture.
Chinese patent application numbers 200810029463.5, July 15 2008 applying date, open day on February 25th, 2009, name is called: " a kind of method of utilizing the palladium film to produce high-purity hydrogen from hydrogen containing synthesis gas ", this patent application disclose a kind of method of producing high-purity hydrogen from hydrogen containing synthesis gas.May further comprise the steps: (1) at first enters water cooler from the synthetic gas that contains water vapor and hydrogen of upstream hydrogen-manufacturing reactor production, is reduced to 75～85 ℃, and the synthetic gas after the cooling enters gas-liquid separator, separates with synthetic gas behind the water vapor condensation; (2) synthetic gas after dewatering enters primary heater, and synthetic gas is heated to 250～350 ℃ in well heater; Be heated the back synthetic gas and enter secondary heater, synthetic gas is heated to 450～600 ℃; (3) heated synthetic gas enters the palladium membrane separation apparatus, and the most of hydrogen in the synthetic gas sees through the palladium membrane separation apparatus becomes high purity product hydrogen.This production method synthetic gas need be heated to comparatively high temps, has the technical problem that energy consumption is higher, equipment is complicated, investment is big.
Summary of the invention
In order to overcome the defective of prior art, technical problem to be solved by this invention is, provide a kind of simple in structure, hydrogen pressure-losses in treating processes is low, energy consumption is low, good product quality, the production of sodium chlorate byproduct hydrogen cleaning that safety performance is high and the method for conveying.
In order to solve the problems of the technologies described above, the basic technical scheme that the present invention adopts is:
A kind of hydrogen cleaning and carrying method, may further comprise the steps: the gas mixture that contains water vapor and hydrogen that (1) obtains from the production of sodium chlorate process is sent into water cooler, the temperature of gas mixture is cooled to 5～15 ℃, gas mixture after the cooling enters gas-liquid separator, with mixed gas separation, water of condensation enters in the water seal behind the water vapor condensation; (2) gas mixture after step (1) enters absorbent charcoal adsorber, further adsorbs the moisture in the gas mixture; (3) gas mixture after step (2) is sent into the dry-seal gasholder storage, and air storage pressure is 2.5kP～3.5kP; Send outside after gas send compressor compresses to 0.55～0.6mpa in the dry-seal gasholder.
Preferably be provided with water seal on described dry-seal gasholder intake ducting and outlet pipe, the water level by in the control water seal can switch on or off the conveying of hydrogen.
Preferably on dry-seal gasholder intake ducting and outlet pipe, be provided with the condensed water discharge pipe road, in the gas delivery process, the water of condensation in the pipeline entered in the water seal.
Be preferably refrigerated cooler at the water cooler described in the step (1), advance the water cooler chilled liquid temperature and be preferably 3 ℃～7 ℃.
The invention has the beneficial effects as follows: solved the technical problem of entrapped moisture in the hydrogen, improved the purity of hydrogen, reduced the maintenance cost of hydrogen pressure machine, prolonged the work-ing life of palladium catalyst, the regular supply and the device continuous production of hydrogen have been ensured, help safe and stable arrangement production, adopt water seal arrangement, system safe, pipeline carries pressure drop little, the multichannel condensate water extraction device is installed, help the timely discharge of water of condensation in each process, adopt first frozen cooling to dewater, utilize the mode of charcoal absorption again, help prolonging the time of regeneration of activated carbon, reduce production costs, system architecture is simple, but safe, pressure drop is less in the course of conveying, helps energy-conservation.
Description of drawings
Fig. 1 is a technical process schematic flow sheet of the present invention.
1, be that water cooler, 2 is that gas-liquid separator, 3 is that absorbent charcoal adsorber, 4 is that dry-seal gasholder import water seal, 5 is that dry-seal gasholder, 6 is that air compressor machine, 8,9,10,11 is water seal for dry-seal gasholder exports water seal, 7.
Embodiment
Below in conjunction with accompanying drawing the specific embodiment of the present invention is elaborated.
Embodiment 1:
The hydrogen mixed gas that contains water vapor that from the production of sodium chlorate process of upstream, obtains, pressure with 15～25KPa enters the refrigerated water water cooler, feed 3 ℃ water coolant in the refrigerated water water cooler, mixture temperature is reduced to 5 ℃, gas mixture after the cooling enters gas-liquid separator, behind the water vapor condensation with mixed gas separation, water of condensation enters in the water seal, lowest point at each pipeline of gas delivery, be provided with the condensed water discharge pipe road, water of condensation in the pipeline is entered in the water seal, further reduce the moisture content in the gas; Gas mixture behind the refrigerated water water cooler cooling de-watering enters absorbent charcoal adsorber, further adsorption moisture and impurity; After above processing, entering dry-seal gasholder stores, dry-seal gasholder intake ducting and outlet pipe are provided with water seal, by the water level in the control water seal, can switch on or off the conveying of hydrogen, the security of raising system, air storage pressure are to send outside after gas send compressor compresses to be pressurized to 0.55～0.6MPa in the 2.5KPa dry-seal gasholder.
Embodiment 2:
The hydrogen mixed gas that contains water vapor that from the production of sodium chlorate process of upstream, obtains, pressure with 15～25KPa enters the refrigerated water water cooler, feed 5 ℃ water coolant in the refrigerated water water cooler, mixture temperature is reduced to 9 ℃, gas mixture after the cooling enters gas-liquid separator, behind the water vapor condensation with mixed gas separation, water of condensation enters in the water seal, lowest point at each pipeline of gas delivery, be provided with the condensed water discharge pipe road, water of condensation in the pipeline is entered in the water seal, further reduce the moisture content in the gas; Gas mixture behind the refrigerated water water cooler cooling de-watering enters absorbent charcoal adsorber, further adsorption moisture and impurity; After above processing, entering dry-seal gasholder stores, dry-seal gasholder intake ducting and outlet pipe are provided with water seal, by the water level in the control water seal, can switch on or off the conveying of hydrogen, the security of raising system, air storage pressure are to send outside after gas send compressor compresses to be pressurized to 0.55～0.6MPa in the 3.0KPa dry-seal gasholder.
Embodiment 3:
The hydrogen mixed gas that contains water vapor that from the production of sodium chlorate process of upstream, obtains, pressure with 15～25KPa enters the refrigerated water water cooler, feed 4 ℃ water coolant in the refrigerated water water cooler, mixture temperature is reduced to 7 ℃, gas mixture after the cooling enters gas-liquid separator, behind the water vapor condensation with mixed gas separation, water of condensation enters in the water seal, lowest point at each pipeline of gas delivery, be provided with the condensed water discharge pipe road, water of condensation in the pipeline is entered in the water seal, further reduce the moisture content in the gas; Gas mixture behind the refrigerated water water cooler cooling de-watering enters absorbent charcoal adsorber, further adsorption moisture and impurity; After above processing, entering dry-seal gasholder stores, dry-seal gasholder intake ducting and outlet pipe are provided with water seal, by the water level in the control water seal, can switch on or off the conveying of hydrogen, the security of raising system, air storage pressure are to send outside after gas send compressor compresses to be pressurized to 0.55-0.6MPa in the 3.5KPa dry-seal gasholder.
Embodiment 4:
The hydrogen mixed gas that contains water vapor that from the production of sodium chlorate process of upstream, obtains, pressure with 15～25KPa enters the refrigerated water water cooler, feed 6 ℃ water coolant in the refrigerated water water cooler, mixture temperature is reduced to 10 ℃, gas mixture after the cooling enters gas-liquid separator, behind the water vapor condensation with mixed gas separation, water of condensation enters in the water seal, lowest point at each pipeline of gas delivery, be provided with the condensed water discharge pipe road, water of condensation in the pipeline is entered in the water seal, further reduce the moisture content in the gas; Gas mixture behind the refrigerated water water cooler cooling de-watering enters absorbent charcoal adsorber, further adsorption moisture and impurity; After above processing, entering dry-seal gasholder stores, dry-seal gasholder intake ducting and outlet pipe are provided with water seal, by the water level in the control water seal, can switch on or off the conveying of hydrogen, the security of raising system, air storage pressure are to send outside after gas send compressor compresses to be pressurized to 0.55-0.6MPa in the 3.2KPa dry-seal gasholder.
Among the above embodiment, the moisture content of gas mixture during by air inlet≤0.5%, after system handles, be reduced to≤0.1% gas mixture hydrogen content 〉=98.5% that obtains, oxygen level≤0.4%, other inert substance content≤1% can satisfy the requirement of producing hydrogen peroxide; The intake pressure of gas mixture is 15～25KPa, is 2.5～3.5 Kpa to the pressure of gas holder, and in treating processes, the pressure of gas mixture is lower, and pressure loss is less, helps energy-conservation.
Obviously, the invention is not restricted to above preferred implementation, also can in spirit of the present invention, change other processing condition, have same effect, so do not repeat.Those of ordinary skill in the art can from content disclosed by the invention directly or all methods of associating also belong to protection scope of the present invention.
Claims (4)
1. hydrogen cleaning and carrying method is characterized in that: may further comprise the steps:
Step 1, the gas mixture that contains water vapor and hydrogen that obtains from the production of sodium chlorate process are sent into water cooler, the temperature of gas mixture is cooled to 5～15 ℃, gas mixture after the cooling enters gas-liquid separator, and with mixed gas separation, water of condensation enters in the water seal behind the water vapor condensation;
Step 2, the gas mixture after step 1 enter absorbent charcoal adsorber, further adsorb the moisture in the gas mixture;
Step 3, the gas mixture after step 2 are sent into dry-seal gasholder and are stored, and air storage pressure is 2.5kP～3.5kP; Send outside after gas send compressor compresses to 0.55～0.6mpa in the dry-seal gasholder.
2. hydrogen cleaning according to claim 1 and carrying method is characterized in that: described dry-seal gasholder intake ducting and outlet pipe are provided with water seal, and the water level by in the control water seal can switch on or off the conveying of hydrogen.
3. hydrogen cleaning according to claim 1 and 2 and carrying method is characterized in that: be provided with the condensed water discharge pipe road on dry-seal gasholder intake ducting and outlet pipe, in the gas delivery process, the water of condensation in the pipeline entered in the water seal.
4. hydrogen cleaning according to claim 1 and carrying method is characterized in that: the water cooler described in the step 1 is the refrigerated water water cooler, and advancing the water cooler chilled water temperature is 3 ℃～7 ℃.
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| CN 201010508091 CN101982403A (en) | 2010-10-15 | 2010-10-15 | Hydrogen purification and transportation method |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102491272A (en) * | 2011-12-09 | 2012-06-13 | 华东理工大学 | Process and device for purifying high-purity hydrogen |
| CN106591874A (en) * | 2016-12-09 | 2017-04-26 | 海南金海浆纸业有限公司 | System and method for comprehensively utilizing chlorate electrolysis hydrogen |
| CN107915208A (en) * | 2017-12-14 | 2018-04-17 | 佛山市天宇鸿图创新科技有限公司 | A kind of novel energy-conserving hydrogen reclaimer |
| CN109224753A (en) * | 2018-09-30 | 2019-01-18 | 新疆泓森环境工程有限公司 | Fluid pressure type gas compression purification system and its compression purification method |
| CN110052113A (en) * | 2019-05-23 | 2019-07-26 | 河南开祥精细化工有限公司 | A method of for reducing carbonyl nickel content in low pressure reaction tail gas |
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| CN1994525A (en) * | 2006-12-11 | 2007-07-11 | 唐莉 | Method for separating and reclaiming hydrogen from chloroethylene or chlor-alkali production exhaust |
| CN101648698A (en) * | 2009-08-31 | 2010-02-17 | 济南德洋特种气体有限公司 | Preparation method of high purity hydrogen |
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2010
- 2010-10-15 CN CN 201010508091 patent/CN101982403A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1994525A (en) * | 2006-12-11 | 2007-07-11 | 唐莉 | Method for separating and reclaiming hydrogen from chloroethylene or chlor-alkali production exhaust |
| CN101648698A (en) * | 2009-08-31 | 2010-02-17 | 济南德洋特种气体有限公司 | Preparation method of high purity hydrogen |
Non-Patent Citations (2)
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| 《中国氯碱》 19971231 阎海洁 氯氢处理工序氢气***改造的体会 14-15 1-4 , 第9期 2 * |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102491272A (en) * | 2011-12-09 | 2012-06-13 | 华东理工大学 | Process and device for purifying high-purity hydrogen |
| CN102491272B (en) * | 2011-12-09 | 2013-04-17 | 华东理工大学 | Process and device for purifying high-purity hydrogen |
| CN106591874A (en) * | 2016-12-09 | 2017-04-26 | 海南金海浆纸业有限公司 | System and method for comprehensively utilizing chlorate electrolysis hydrogen |
| CN106591874B (en) * | 2016-12-09 | 2019-02-26 | 海南金海浆纸业有限公司 | A kind of utilization system and its method of comprehensive utilization of chlorate electrolysis hydrogen |
| CN107915208A (en) * | 2017-12-14 | 2018-04-17 | 佛山市天宇鸿图创新科技有限公司 | A kind of novel energy-conserving hydrogen reclaimer |
| CN109224753A (en) * | 2018-09-30 | 2019-01-18 | 新疆泓森环境工程有限公司 | Fluid pressure type gas compression purification system and its compression purification method |
| CN110052113A (en) * | 2019-05-23 | 2019-07-26 | 河南开祥精细化工有限公司 | A method of for reducing carbonyl nickel content in low pressure reaction tail gas |
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Application publication date: 20110302 |