CN1331732C - Process and apparatus for preparing hihg-purity CO, hydrogen and their mixture by cracking methanol - Google Patents
Process and apparatus for preparing hihg-purity CO, hydrogen and their mixture by cracking methanol Download PDFInfo
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- CN1331732C CN1331732C CNB011401389A CN01140138A CN1331732C CN 1331732 C CN1331732 C CN 1331732C CN B011401389 A CNB011401389 A CN B011401389A CN 01140138 A CN01140138 A CN 01140138A CN 1331732 C CN1331732 C CN 1331732C
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- methanol
- gas
- hydrogen
- methyl alcohol
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
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Abstract
The present invention relates to a method for preparing high-purity carbon monoxide, hydrogen and mixtures thereof through methanol cracking. Methanol liquid is gasified and overheated at first; at a certain temperature, methanol is cracked into mix gas containing CO, CO2 and H2 through the catalytic action of special catalysts; then, CO2 is eliminated by an alkali washing method or a pressure swing adsorption (PSA) method; by the pressure swing adsorption (PSA) method and different adsorbing agents, 99.9% of H2 and 99.9% of CO can be obtained. The device of the present invention comprises a methanol metering and pressurizing device, a methanol gasifying device, a catalytic reactor, a heat exchanger, a CO2 eliminating device and a product gas purifying device.
Description
Technical field
The present invention relates to a kind of method and apparatus for preparing carbon monoxide, hydrogen and composition thereof, particularly a kind of method and apparatus for preparing splitting gas and usefulness pressure swing adsorption process refined product gas with catalytic pyrolysis methyl alcohol.
Background technology
Carbon monoxide is widely used in the organic synthesis as a kind of extraordinary industrial gas raw material, produces phosgene, and the preparation methylcarbonate is as the intermediate of medical agricultural chemicals etc.Usually, carbon monoxide is to be raw material with coal, coke, utilizes producer gas generator to produce CO, H
2, CO
2, N
2, O
2Deng mixed gas, utilize two sections pressure swing adsorption processs (PSA) or step chemical method of purification to obtain the product CO (carbon monoxide converter) gas again.Because mixed gas except that above-mentioned inorganic component, also contains a spot of tar and sulfocompound, causes the gaseous fraction complexity, the isolation of purified long flow path.Therefore the output that the purity of utilizing the chemical purification method to obtain is higher than 99.9% carbon monoxide is very little, causes cost bigger, and price is very high.And adopt the purity of the industrial carbon monoxide of two sections pressure swing adsorption processs purifications generally also can only reach 98%, it is just quite difficult to desire to want to produce more highly purified carbon monoxide.
Summary of the invention
The object of the present invention is to provide a kind of method of utilizing methanol decomposition to prepare high-purity carbon monooxide, hydrogen and mixed gas thereof.The present invention also provides the device of corresponding aforesaid method.
The method that methanol decomposition of the present invention prepares high-purity carbon monooxide, hydrogen and composition thereof comprises the following steps: (1) pre-treatment:, vaporization, overheated pressurised metered to methyl alcohol, obtain temperature between 220 ℃～270 ℃, the methanol gas of pressure in 0.6～2.0Mpa scope; (2) reaction: step (1) Gu the methanol gas that obtains is introduced gas---catalyticreactor, is carried out the scission reaction of methyl alcohol under the effect of catalyzer, contained: CO:26%～30%; CO
2: 1%～3%; CH
4: 0.1～1%; H
2: 66%～73% reforming gas; (3) heat exchange: the thermal transition gas that step (2) is obtained is introduced interchanger, carries out heat exchange with methyl alcohol in the step (1), reduces the temperature of reforming gas, improve the temperature of methyl alcohol, and condensation reduces the temperature of reforming gas; (4) remove CO
2: the CO in the reforming gas that step (3) is obtained
2Remove; (5) purify: the reforming gas that step (4) obtains is purified, obtain corresponding product gas.
In the method for the invention described above, material benzenemethanol there is not particular requirement, as long as meet the quality index of the acceptable end product of GB-388-92.
Catalyzer of the present invention is a solid catalyst, and main effective constituent is CuO, in addition, also contains ZnO, Al
2O
3And Cr
2O
3Wherein, ZnO is a promotor, Al
2O
3And Cr
2O
3Be support of the catalyst.Be with Cu (NO
3)
2, Zn (NO
3)
2, Al (NO
3)
3Solution and Na
2CO
3Reaction produces precipitation, grinds material through filtration, oven dry back, adds chromic anhydride when the stone roller material, through granulation, roasting, the moulding of adding graphite.
The katalysis of above-mentioned catalyzer is: CuO is reduced into Cu at a certain temperature, it is main catalyst component, can accelerate the speed of response of methanol decomposition, methanol gas is adsorbed by Cu through beds the time, following dehydrogenation reaction takes place under the effect of catalyzer
CH
3OH→CO+2H
2-Q
The CO and the H that generate
2And unreacted CH
3OH enters main air stream after taking off absorption from catalyzer, through condensation separation CH
3Behind the OH, obtain product gas.ZnO exists as promotor in above-mentioned catalyzer, can further promote the katalysis of Cu.Because this catalyzed reaction is a strong endothermic reaction, must carry out, and Cu crystal grain when temperature is higher rises greatly easily, influence the stable of katalysis, the Al in the catalyzer under comparatively high temps
2O
3And Cr
2O
3Have better heat-resisting, and can uniformly separately keep the stable of katalysis Cu crystal grain.
Methanol decomposition temperature of the present invention is between 230～260 ℃, and cracking pressure is grasped in the scope of 0.6～2.0Mpa.
The step of the method for the invention described above removes CO in (4)
2Method comprise alkali wash and PSA pressure swing adsorption process, remove the back CO
2Content below 0.5%.
The method of the refined product gas in the step of the method for the invention described above (5) comprises the PSA pressure swing adsorption process, can obtain the CO of 99.9% hydrogen and 99.9% respectively by filling different sorbent materials.
The method for preparing high-purity carbon monooxide, hydrogen and composition thereof at the invention described above methanol decomposition, the device that the present invention also provides a kind of methanol decomposition to prepare high-purity carbon monooxide, hydrogen and composition thereof comprises methyl alcohol metering pressurizing device, methyl alcohol vapourizing unit, catalyticreactor, heat exchanger, takes off CO
2Device, product device purifying plant.
The pressurised metered device of above-mentioned methyl alcohol comprises metering force (forcing) pump and methanol purity detector and transfer line and by-pass valve control, and the metering force (forcing) pump pumps into methanol liquid from the methyl alcohol holding tank, and the methanol purity detector is monitored the purity of key alcohol in real time; The methyl alcohol heating and vaporizing device comprises vaporizer and corresponding pipeline, and described vaporizer can be a tubular heater exchhanger; Gu the methyl alcohol catalyticreactor is a gas a---catalytic bed, in catalyzer is housed; Heat exchanger can be a tubular heater exchhanger; Take off CO
2Device can be washing tower or adsorption tower; Product gas purifying plant is the PSA adsorption tower, and adsorption tower is four towers, and sorbent material is arranged in the tower.
Take off CO
2Device can be that washing device can be an adsorption unit also, is techniques well known, needn't state more.
The PSA sorbent material can be H
2Sorbent material also can be the CO sorbent material, decides on the kind and the specification of quality of product gas.
The present invention adopts the method for methanol decomposition to produce gas mixture, and this gas mixture does not contain contained tar of carbonization of coal and sulfocompound, purifies and separates than being easier to; Adopt the PSA pressure swing adsorption process, can obtain different products by using different sorbent materials.Not only can reduce the cost of product gas, can also improve the purity of product gas.
Description of drawings
Fig. 1 is the process flow sheet of the inventive method;
Fig. 2 is a methanol decomposition device synoptic diagram of the present invention;
Fig. 3 is the CO that takes off of the embodiment of the invention
2The device synoptic diagram;
Fig. 4 is the CO that takes off of another embodiment of the present invention
2The device synoptic diagram;
Fig. 5 is CO of the present invention, H
2The purifying plant synoptic diagram.
Embodiment
As shown in Figure 1, be the process flow sheet of the inventive method.Liquid starting material methyl alcohol is after pressurised metered pump pressurization, and the pressure that makes liquid methanol is 0.8～1.2Mpa; Then liquid methanol enters the gasification superheater and heats up and gasify, and makes methanol gas have the temperature between 220 ℃～270 ℃ and the pressure of 0.6～2.0Mpa scope; The methanol gas that will have said temperature and pressure is then introduced catalyticreactor, and following scission reaction takes place in catalyticreactor:
CH
3OH→CO+2H
2-Q
Temperature is grasped between 230～260 ℃ during reaction, and pressure is grasped in the scope of 0.6～2.0Mpa, is converted into CO, H after the reaction
2, CO
2, also contain the unconverted CH of part in addition
3OH; Above-mentioned blended reforming gas is introduced into interchanger and carries out heat exchange, below the temperature to 40 of condensation reforming gas ℃, the unreacted methanol condensation of gas is separated; Reforming gas after the condensation separation enters CO
2Remove device and remove CO
2Remove CO
2Reforming gas obtaining product gas through PSA transformation absorption.
Be specifically described with embodiment below:
Embodiment one:
In device as shown in Figure 2, carry out the cracking of methyl alcohol.The liquid methanol of purity＞99.8% is stored in the methyl alcohol storage tank 1, through pressurised metered pump 2 pressurised metered after, enter gasifier 3, it is overheated to carry out heating and gasifying in gasifier 3, temperature and pressure with the rising methanol gas, obtain temperature between 220～250 ℃, the methanol gas of pressure between 0.8～2.0Mpa.Gu the methanol gas that obtains enters gas again---carry out catalytic conversion reaction in the catalytic bed reactor 4, temperature of reaction is grasped between 230～260 ℃, and reaction pressure is grasped in the scope of 0.6～2.0Mpa, obtains reforming gas.The reforming gas of this moment contains 26～30% CO, 1～3% CO
2, 0.1～1% CH
4, 66～73% H
2With unconverted part methyl alcohol.The reforming gas temperature of this moment is also very high, for making full use of this part heat, can carry out heat exchange with this reforming gas and material benzenemethanol, and the material benzenemethanol temperature is raise and preheating, and the reforming gas temperature reduces.Reforming gas after over-heat-exchanger 5 heat exchanges is again through condensation, and temperature can be reduced to 40 ℃, and under this temperature, unconverted methanol condensed becomes liquid to separate from reforming gas in gas-liquid separation device 6 in the reforming gas.
Reforming gas through above-mentioned processing also contains CO
2, therefore need remove CO
2Process.Present embodiment is deviate from CO
2Device as shown in Figure 4, wherein, the 10th, adsorption tower 1,12 is an adsorption tower 2,11st, by-pass valve control.Be to utilize PSA two tower absorption methods to remove CO
2, utilize the alternate operation vacuum desorption to remove CO
2, and CO
2Sorbent material can adopt existing sorbent material, there is no particular requirement (as: silica gel or activated carbon etc.), and the absorption sequential sees Table 1.
Table 1
| Adsorption tower 1 | A | E1D | D | V | E1R | |
| Adsorption tower 2 | D | V | E1R | A | E1D | |
Wherein: A is an adsorption process; D is the reverse pressure process of putting; V is a vacuum; E1D is equal step-down process once; E1R is the process of once all boosting.
As shown in Figure 5, remove CO
2Reforming gas in CO
2Content reduces to＜and 0.5%, this reforming gas is introduced the PSA adsorption unit of a cover four tower alternate operations, wherein 13,14,15,16 is respectively adsorption tower, and H is housed in the adsorption tower
2Sorbent material (as: zeolite molecular sieve etc.), carry out PSA absorption, in adsorption process, utilize sequence controller, by changing some or a plurality of time variables, can automatic-adjusting device operation situation and obtain the product of different purity, present embodiment absorption control process is as shown in table 2, by the time sequential routine of each tower PSA of time variable control with along putting exhausted air quantity, can obtain 99.9% pure hydrogen at cat head, the draws air at the bottom of tower obtains H
2: CO=1: 1～1: the synthetic gas of 1.5 (V/V), and can finish obtaining simultaneously to two kinds of products.
Embodiment two:
The preparation method of reforming gas is identical with embodiment one in the present embodiment, obtains reforming gas by cracking process.
As shown in Figure 3, remove CO
2Method take the alkali wash of two tower alternate operations, using washing lotion is the NaOH aqueous solution of 10～20% concentration, finishes washing respectively in soda-wash tower 8,9, removes CO
2, in gas-liquid separator 7, separate the liquid that reforming gas is brought into then in washing process.
As shown in Figure 5, remove CO
2Reforming gas purify, purify and adopt the method for PSA four tower alternate operations, filling CO sorbent material in adsorption tower, this sorbent material has copper activity, can carry out chemisorption and physical adsorption simultaneously, specifically can use the PU-1 of pioneer Science and Technology Ltd. of Beijing University, this product has obtained Chinese patent, the patent No. is 86102838, United States Patent (USP) 4917711 and Canadian Patent 1304343, and the quality index of sorbent material sees Table 3:
Table 3
| Adsorptive capacity | Under 25 ℃, CO dividing potential drop 1 normal atmosphere＞46ml/g (static state) |
| Granularity | φ2.0±0.5mm |
| Bulk density | 0.95±0.05kg/l |
| Specific heat | ～0.2 card/gram degree |
| Specific surface | 800m 2/g |
| Crushing strength | ＞5kg/cm |
This adsorption process is at 70 ℃, 0.6 carry out under the condition of～2.0Mpa, program is adjusted the time sequential routine of PSA, all there is adsorption tower to be in adsorbed state any time, other three tower is in different desorption state, the control adsorption cycle is between 12～28 minutes, and the absorption sequential sees Table 2, can make the purity of CO product gas reach 99.9% level.
The above embodiments can also have the combination of different methods, remove CO as also can utilize caustic washing method in embodiment one
2Also can in embodiment two, change the kind of PSA sorbent material and obtain 99.9% pure hydrogen.
Therefore the foregoing description only is to specifying that the present invention makes, and can not limit various form of the present invention with the foregoing description.Protection scope of the present invention should be as the criterion with claims institute restricted portion.
Table 2
| 1 | 2 | 3 | 4 | |||||||||||||||||
| A | A | E1D | E2D | PP | D | V | E2R | E1R | FR | |||||||||||
| B | E1R | FR | A | E1D | E2D | PP | D | V | E2R | |||||||||||
| C | V | E2R | E1R | FR | A | E1D | E2D | PP | D | V | ||||||||||
| D | E1D | E2D | PP | D | V | E2R | E1R | FR | A | |||||||||||
Wherein, A is an adsorption process; E1D is equal step-down process once; E2D is the equal step-down process of secondary; PP is the suitable journey of letting slip; P is a flushing process; D is the reverse pressure process of putting; V is a vacuum; E1R is the process of once all boosting; E2R is the secondary process of all boosting; FR is for filling eventually.
Claims (8)
1. a methanol decomposition prepares the method for high-purity carbon monooxide, hydrogen and composition thereof, comprises the following steps:
(1) pre-treatment: pressurised metered to methyl alcohol, the vaporization overheated, obtain temperature between 220 ℃～270 ℃, the methanol gas of pressure in 0.6～2.0Mpa scope;
(2) reaction: above-mentioned methanol gas introducing is contained CuO, ZnO, Al
2O
3And Cr
2O
3The catalyticreactor of solid catalyst in, under the effect of catalyzer, carry out the scission reaction of methyl alcohol, obtain containing CO, CO
2, CH
4, and H
2Reforming gas;
(3) heat exchange: the reforming gas that step (2) obtains is introduced interchanger, carry out heat exchange, reduce the temperature of reforming gas;
(4) take off CO
2: the CO in the reforming gas that step (3) is obtained
2Remove;
(5) purify: the reforming gas that step (4) obtains is purified, obtain corresponding product gas.
2. methanol decomposition according to claim 1 prepares the method for high-purity carbon monooxide, hydrogen and composition thereof, it is characterized in that: this catalyzer is with Cu (NO
3)
2, Zn (NO
3)
2, Al (NO
3)
3Solution and Na
2CO
3Reaction produces precipitation, grinds material through filtration, oven dry back, adds chromic anhydride when the stone roller material, makes through granulation, roasting, the moulding of adding graphite.
3. methanol decomposition according to claim 1 prepares the method for high-purity carbon monooxide, hydrogen and composition thereof, it is characterized in that: remove CO
2Method comprise alkali wash or pressure swing adsorption process.
4. prepare the method for high-purity carbon monooxide, hydrogen and composition thereof according to claim 1 or 3 described methanol decompositions, it is characterized in that: the method for purification reforming gas comprises pressure swing adsorption process.
5. a device that uses methanol decomposition as claimed in claim 1 to prepare the method for high-purity carbon monooxide, hydrogen and composition thereof is characterized in that: comprise that the methyl alcohol that connects successively measures pressurizing device, methyl alcohol vapourizing unit, catalyticreactor, heat exchanger, takes off CO
2Device, product gas purifying plant.
6. device according to claim 5, it is characterized in that: this takes off CO
2Device is two tower alkaline cleaners.
7. device according to claim 5, it is characterized in that: this takes off CO
2Device is two tower pressure-swing absorption apparatuss.
8. device according to claim 5 is characterized in that: this product gas purifying plant is four tower pressure-swing absorbers.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011401389A CN1331732C (en) | 2001-11-27 | 2001-11-27 | Process and apparatus for preparing hihg-purity CO, hydrogen and their mixture by cracking methanol |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011401389A CN1331732C (en) | 2001-11-27 | 2001-11-27 | Process and apparatus for preparing hihg-purity CO, hydrogen and their mixture by cracking methanol |
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| Publication Number | Publication Date |
|---|---|
| CN1346786A CN1346786A (en) | 2002-05-01 |
| CN1331732C true CN1331732C (en) | 2007-08-15 |
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|---|---|---|---|
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| CN1297476C (en) * | 2005-02-01 | 2007-01-31 | 北京科技大学 | Method for preparing nanometer tungsten carbide powder by methyl alcohol cracking |
| CN100427382C (en) * | 2006-09-10 | 2008-10-22 | 郑国璋 | Heating to conatant temperature type equipment for reloading methanol |
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| CN105861073A (en) * | 2016-06-01 | 2016-08-17 | 北京神雾环境能源科技集团股份有限公司 | Method and system for purifying CO fuel gas through continuous pyrolysis of carbon-containing organic matter |
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|---|---|
| CN1346786A (en) | 2002-05-01 |
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Owner name: SICHUAN YALIAN HIGH-TECH CO., LTD. Free format text: FORMER NAME: SICHUAN YALIAN HIGH-TECH CO.,LTD. |
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Address after: No. 5 high tech Zone Gaopeng road in Chengdu city of Sichuan Province Patentee after: Sichuan Ally Hi-tech Co., Ltd. Address before: High tech Zone Gaopeng Avenue in Chengdu city in Sichuan province No. 5, park B block, floor 4 Patentee before: Yalian High-Tech Co., Ltd., Sichuan |
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Granted publication date: 20070815 Termination date: 20161127 |