CN104857817A - Low temperature methanol washing gas stripping regeneration methyl alcohol equipment and utilization method thereof - Google Patents
Low temperature methanol washing gas stripping regeneration methyl alcohol equipment and utilization method thereof Download PDFInfo
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- CN104857817A CN104857817A CN201510242607.5A CN201510242607A CN104857817A CN 104857817 A CN104857817 A CN 104857817A CN 201510242607 A CN201510242607 A CN 201510242607A CN 104857817 A CN104857817 A CN 104857817A
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Abstract
The invention discloses low temperature methanol washing gas stripping regeneration methyl alcohol equipment and a utilization method thereof. The equipment is arranged between a methyl alcohol washing tower and a gas stripping regeneration tower; a purified gas outlet drain is arranged on a purified gas outlet pipeline at the top of the methyl alcohol washing tower; a downstream end of the purified gas outlet drain is communicated with the bottom of the gas stripping regeneration tower and the other end is connected with a nitrogen source. When the nitrogen source cannot provide nitrogen, the equipment enables purified gas at the top of the methyl alcohol washing tower to pass through the opening purified gas outlet drain and be reduced pressure through a reducing valve and lead to the gas lifting regeneration tower to serve as gas stripping gas to regenerate the methyl alcohol. Accordingly, under the nitrogen source fault condition, ceaseless operation of the gas lifting regeneration tower is guaranteed, continuous operation of a low temperature methanol washing step is guaranteed, an air separation device is not required to be introduced, and economic losses are reduced.
Description
Technical field
The present invention relates in ammonia synthesis process, after conversion gas low-temperature rectisol, the production technology of Mathanol regenerating, is equipment and the using method thereof of air lift regenerated methanol after a kind of low-temperature rectisol concretely.
Background technology
In Ammonia Production, low-temp methanol washing process is adopted for conversion gas purification, that is: utilizes methyl alcohol absorbing carbon dioxide (CO under low temperature
2), hydrogen sulfide (H
2s) and organic sulfur impurity as sulphur carbonoxide (COS) etc.; Also remove the saturation water brought in change gas, obtained qualified purified gas is sent to methanol-fueled CLC post or liquid nitrogen washing post simultaneously.After low-temp methanol wash-out is complete, before again recycling, have to pass through air lift regeneration.Normally by the methyl alcohol after wash-out after decompression is resolved, import the gas of inertia, reduce solute (impurity of absorption) dividing potential drop, realize carrying out air lift, make Mathanol regenerating.
Above process based on principle be: the principle of low-temperature rectisol, specific as follows:
The process of methanol absorption sour gas does not have chemical reaction to occur, and therefore belongs to Physical Absorption.The theoretical foundation of this Physical Absorption is---Henry's law, and its expression formula is:
P＝KX
In formula: P-operating pressure; K-Henry'S coefficient; The molecular fraction of X-solute.
Find out from formula: the higher then X of P is larger, represent dissolving solute in a solvent the more.
The large and small of K value is also different with the difference of solute, solvent.Solvent methanol molecule is polar molecule, therefore to the solute CO being polar molecule equally
2, H
2the uptake of S etc. just belongs to the H of nonpolar molecule much larger than molecule
2, N
2, CO, Ar (this type of gas is thought " gas of inertia ") etc. uptake.Anticipate namely: solvent methanol is to solute CO
2, H
2s and solvent methanol are to solute H
2, N
2, CO, Ar etc. K value be different.
When solvent absorbs, higher according to Henry's law pressure, temperature is lower, the solute amount that unit solvent amount absorbs also the more, therefore, when absorbing, desirably high pressure, low temperature.Due under high pressure, low temperature, gas has been actual gas, therefore not exclusively follows Henry's law, namely must revise Henry's law.But the absorption of solvent to solute still has following trend:
1) for majority of gas, pressure is higher, temperature is lower; Rule of thumb, absorb temperature then usually to exceed than the dew-point temperature of feed gas: be advisable for 5 ~ 10 DEG C.
2) under the condition of actual gas, each intermolecular in mist also exists gravitation, i.e. Van der Waals force, and it reduces making its meltage in a solvent and also the dew point of mist declined to some extent than pure gas.
3) for mist, when a kind of easily dissolved component dissolves in a solvent, this diffluent component can absorb another component as solvent.
When the solvent absorbing solute carries out desorb: lower according to Henry's law pressure, temperature is higher, then be more beneficial to the desorb of solute, when temperature equals the boiling point of solvent, solute meltage is in a solvent zero.Therefore, the method for selective solvent desorb has:
1) reduce pressure desorption method, namely absorbs the solvent of solute, by throttling and the stagnation pressure (even arriving negative pressure) reducing system, realizes the desorb of solute.
2) air lift desorption method, namely imports the gas of inertia, reduces solute dividing potential drop, realizes the desorb of solute.
3) heating desorption method, namely with external heat solvothermal to boiling, make solute meltage in a solvent be zero.
Based on above discussion, the flow process of low-temperature rectisol operation consists of: the sour gas in methanol absorption conversion gas, adopts pressurizing absorption; Absorbing temperature for reducing, the rich methanol absorbing sour gas, adopting first precooling to reduce pressure again desorb, to obtain lower system temperature, and by exchange heat, the absorption temperature of clean methyl alcohol being reduced.For ensureing that the degree of purification absorbing rear gained Purge gas reaches requirement, finally can also adopt and methyl alcohol is heated to boiling point desorb, the methyl alcohol after desorb, being no longer dissolved with any sour gas.
In ammonia synthesis process, modal inert gas is nitrogen, and low-temperature rectisol step just adopts nitrogen as gas stripping gas.During the device full production of a set of low-temperature rectisol, required nitrogen amount is 2500m
3about/h, the rate of recovery about 70% of usual carbon dioxide.
If do not carry out air lift to the methyl alcohol absorbing foreign gas, so this methyl alcohol cannot remove absorbing carbon dioxide and hydrogen sulfide again; And then causing low-temperature rectisol step to be stopped, whole Ammonia Production flow process is interrupted.
In Ammonia Production, must to stop transport the situations such as overhaul if run into coal gasification apparatus, methyl alcohol still uses nitrogen as air lift stripping medium.Nitrogen is now provided by a set of air-separating plant.It is 6000m that normally used air-separating plant produces nitrogen designed capacity
3/ h, actual product nitrogen quantity is 4500 ~ 8500m
3/ h, is far longer than nitrogen amount needed for methanol wash column, must process unnecessary nitrogen during use, causes certain waste.Just in case air-separating plant breaks down, can not continue to provide required nitrogen, then also cause low-temperature rectisol step to stop, whole Ammonia Production flow process is interrupted.
When lasting enough nitrogen cannot be provided, how can effectively and economic guarantee low-temperature rectisol step can continuous firing, this is the difficult problem that those skilled in the art generally acknowledge and the direction of making great efforts exploration always, but also there is no the appearance of gratifying technical scheme up to now.
Summary of the invention
The first object of the present invention is exactly the equipment that will provide air lift regenerated methanol after a kind of low-temperature rectisol, this technology can be guaranteed to provide the gas of lasting enough inertia to make gas stripping gas, ensure that low-temperature rectisol step can continuous firing, ensure that the regular regeneration of methyl alcohol and the stable of Ammonia Production technique carry out, relative to direct external air-separating plant more easily and effectively.
For achieving the above object, after the low-temperature rectisol designed by the present invention, air lift regenerated methanol equipment is arranged between Methanol Wash Column and air lift regenerator, comprises equipment and is: on the clean gas outlet pipeline of methanol wash top of tower, arrange clean gas outlet lead pouring; The downstream that described clean gas outlet leads pouring connects purified gas introduction pipe line; Purified gas introduction pipe line access gas stripping gas pipeline; Described gas stripping gas pipeline one end passes into the bottom of air lift regenerator, and the other end connects source nitrogen.
Preferably, described purified gas pipeline is also provided with pressure-reducing valve.
Preferably, close source nitrogen one end of described gas stripping gas pipeline is provided with nitrogen pipeline valve; The end of described gas stripping gas pipeline bottom air lift regenerator is provided with gas stripping gas pipeline valve.
Preferably, the position of described purified gas introduction pipe line access gas stripping gas pipeline is between nitrogen pipeline valve and air lift gas pipeline valve.
Further, on the clean gas outlet pipeline of methanol wash top of tower, be no more than described methanol wash top of tower 10 meters of and described clean gas outlet is set leads pouring.
The second object of the present invention is the using method of the equipment of air lift regenerated methanol after the low-temperature rectisol of design, comprises the steps:
Step 1) source nitrogen be when cannot continue to provide enough nitrogen, opens clean gas outlet and leads pouring, and methanol wash top of tower has Partial cleansing gas to lead to drench by clean gas outlet and flow in purified gas introduction pipe line;
Step 2) regulate pressure-reducing valve, make the pressure of the purified gas flowed out in Methanol Wash Column identical with the desorption pressures in air lift regenerator;
Step 3) regulate the gentle nitrogen flow carried needed for regenerator of purified gas flow of purified gas introduction pipe line consistent;
Step 4) close nitrogen pipeline valve; Purified gas continues to flow in air lift regenerator;
Step 5) when source nitrogen can continue enough the supply of nitrogen again in air lift regenerator, open nitrogen pipeline valve, close clean gas outlet and lead pouring; Enter normal productive process.
Preferably, described step 2) in, pressure-reducing valve 5 by the Pressure Drop of described purified gas to 0.19MPa.
Preferably, described step 3) in, the purified gas flow in purified gas introduction pipe line 2 is 2000 ~ 3000m
3/ h.
The present invention is carefully studying and is analyzing in low-temperature rectisol process and air lift Mathanol regenerating process afterwards, on the basis of the respective physics of methyl alcohol and corresponding gas with various and chemical characteristic, in conjunction with the operation characteristic of low-temperature rectisol and air lift Mathanol regenerating equipment, dexterously purified gas is imported air lift regenerator as gas stripping gas temporarily to replace nitrogen, its advantage is mainly reflected in following several respects:
One, the purified gas stable components that methanol wash top of tower is derived, and relative to being the gas of inertia methyl alcohol.This to utilize purified gas to replace nitrogen as the necessary condition of gas stripping gas.
Its two, finding after purified gas constituent analysis, is that the gas stripping gas of Mathanol regenerating is compared with nitrogen with simple, and the hydrogen occupied the majority in purified gas to regenerate methyl alcohol as gas stripping gas and the effect of carbon dioxide recovery also will be got well.
Its three, the temperature of the purified gas in Methanol Wash Column is lower than the nitrogen temperature of source nitrogen, can more effectively regenerate and carbon dioxide recovery methyl alcohol.
Its four, after low-temperature rectisol designed by the present invention, the equipment of air lift regenerated methanol needs pipeline installation between air lift regenerator and Methanol Wash Column, simultaneously on pipeline, installs various gate and control facility.Do not need the equipment in script ammonia synthesis process to carry out major alteration or transformation, required improvement project amount is little, easy construction, is also easy to apply.
They are five years old, when source nitrogen break down can not lasting enough nitrogen, after utilizing low-temperature rectisol designed by the present invention, the equipment of air lift regenerated methanol can ensure the non-stop run of air lift regenerator, do not need to introduce air-separating plant in addition, neither lose time, can also ensure that processing step uninterruptedly carries out simultaneously, avoid waste.
Its six, the present invention can also be used as the air lift air machinery for subsequent use of air lift regenerator.Other similar techniques can be given to inspire simultaneously.
Accompanying drawing explanation
Fig. 1 is the structural representation of the equipment of air lift regenerated methanol after low-temperature rectisol.
In figure: Methanol Wash Column 1, purified gas introduction pipe line 2, air lift regenerator 3, clean gas outlet leads pouring 4, pressure-reducing valve 5, gas stripping gas pipeline 6, gas stripping gas pipeline valve 7, nitrogen pipeline valve 8.
Detailed description of the invention
Below in conjunction with the drawings and specific embodiments, equipment and process of the present invention is described in further detail.
The equipment of air lift regenerated methanol after low-temperature rectisol as shown in Figure 1, is arranged between Methanol Wash Column 1 and air lift regenerator 3.
The clean gas outlet pipeline at Methanol Wash Column 1 top arranges clean gas outlet and leads pouring 4.The downstream that described clean gas outlet leads pouring 4 connects purified gas introduction pipe line 2.Described purified gas pipeline 2 is also provided with pressure-reducing valve 5.Purified gas introduction pipe line 2 accesses gas stripping gas pipeline 6.
Gas stripping gas pipeline 6 passes into the bottom of air lift regenerator 3.The supplied materials arrival end of described gas stripping gas pipeline 6 is provided with nitrogen pipeline valve 8, and this gas stripping gas pipeline 6 is provided with gas stripping gas pipeline valve 7 near the end of air lift regenerator 3.During normal operation, this gas stripping gas pipeline 6 does gas stripping gas to supplying nitrogen in air lift regenerator 3, methyl alcohol air lift to be regenerated.
When purified gas introduction pipe line 2 accesses gas stripping gas pipeline 6, be arranged between gas stripping gas pipeline valve 7 and nitrogen pipeline valve 8.
Conversion gas is (except main component hydrogen and nitrogen, also containing impurity such as carbon dioxide, hydrogen sulfide, sulphur carbonoxide, carbon monoxide) enter Methanol Wash Column 1 from bottom, low-temp methanol is sent into from the top of Methanol Wash Column 1, the two counter current contacting.The acid gas impurities such as the carbon dioxide in conversion gas, hydrogen sulfide and sulphur carbonoxide are large all by after methanol absorption absolutely, obtain purified gas.The composition of this purified gas is: hydrogen 75V/V%, nitrogen 24.8V/V%, other 0.2V/V% (V/V% is percent by volume).In purified gas, other gases of 0.2V/V% mainly carbon monoxide, do not absorb carbon dioxide, methane etc. completely on a small quantity; The gases such as carbon monoxide wherein and methane are for the gas methyl alcohol being inertia.
The top of Methanol Wash Column 1 is provided with pipeline, to be introduced in subsequent processing by purified gas.In the overhead line of this Methanol Wash Column 1,5 meters of, arrange clean gas outlet and lead pouring 4.This clean gas outlet lead pouring 4 arrange can not exceed this Methanol Wash Column 1 overhead line on 10 meters of.When normally producing, this clean gas outlet leads pouring 4 for closed condition.When the source nitrogen of air lift regenerator 3 is unable to supply, opens this clean gas outlet and lead pouring 4, a part of purified gas can pass through and enter in purified gas introduction pipe line 2.Purified gas introduction pipe line 2 is provided with pressure-reducing valve 5, and 2.88MPa when being flowed out in Methanol Wash Column 1 by the pressure of described purified gas is down to the desorption pressures 0.19MPa of design in air lift regenerator 3.Described purified gas, by after pressure-reducing valve 5, still enters gas stripping gas pipeline 6 along purified gas introduction pipe line 2.The end of described gas stripping gas pipeline 6 is provided with gas stripping gas pipeline valve 7.Described purified gas, by after this gas stripping gas pipeline valve 7, enters bottom air lift regenerator 3, replaces nitrogen as gas stripping gas by Mathanol regenerating.
In normal production, the purified gas output of Methanol Wash Column 1 is 75000m
3/ h; Air lift regenerator 3 needs nitrogen to be 2500m
3/ h.Control to lead the purified gas shunting of flowing out pouring 4, only by 2500m from clean gas outlet
3the purified gas of/h flows in air lift regenerator 3, with alternative nitrogen.
In normal production, the pressure in Methanol Wash Column 1 is 2.88MPa, and the purified gas reset pressure that top is flowed out is 2.88MPa.And the desorption pressures of nitrogen needed for air lift regenerator 3 is 0.19MPa.Therefore, utilize the pressure-reducing valve 5 that purified gas introduction pipe line 2 is installed, purified gas Pressure Drop is low to moderate the desorption pressures 0.19MPa needed for air lift regenerator 3.
In normal production, the bottom of air lift regenerator 3 passes into nitrogen, makes the carbon dioxide desorb in rich methanol.The top of described air lift regenerator 3 is high concentration carbon dioxide recoverer, and bottom is nitrogen air lift portion.Air lift can the most carbon dioxide of desorb.Nitrogen, as gas stripping gas, through recycled for multiple times in this air lift regenerator 3, enters in air as tail gas after eventually passing cold recovery, desulfurization.When utilizing purified gas to substitute nitrogen as gas stripping gas, enter the bottom of air lift regenerator 3 equally through gas stripping gas pipeline 6.Then, purified gas equally with nitrogen can realize air lift, through recycled for multiple times in this air lift regenerator 3, by carbon dioxide desorb; Finally, purified gas is also the same as with nitrogen after the step such as cold recovery, desulfurization, enters in air as tail gas.
Therefore, when in production process, when the nitrogen input bottom air lift regenerator 3 is not enough, namely source nitrogen breaks down or accident, when cannot stablize the enough nitrogen of input continued in air lift regenerator 3, start the equipment of air lift regenerated methanol after the low-temperature rectisol designed by the present invention.After this low-temperature rectisol, the using method of the equipment of air lift regenerated methanol is as the following step:
Step 1) source nitrogen be when cannot continue to provide enough nitrogen, starts this complete equipment.First open clean gas outlet and lead pouring 4, then Methanol Wash Column 1 top has Partial cleansing gas to lead pouring 4 by clean gas outlet to flow in purified gas introduction pipe line 2.Now, the temperature of purified gas is the temperature in Methanol Wash Column 1, namely 20 DEG C.Pressure 2.88MPa (initial pressure) in the pressure ratio Methanol Wash Column 1 of this strand of purified gas is smaller.
Step 2) regulate pressure-reducing valve 5, make the pressure of the purified gas flowed out in Methanol Wash Column 1 identical with the desorption pressures in air lift regenerator 3.Generally, in advance pressure-reducing valve 5 is arranged to the desorption pressures 0.19MPa be decompressed to from the pressure 2.88MPa in Methanol Wash Column 1 in air lift regenerator 3.
Step 3) regulate the gentle nitrogen flow carried needed for regenerator 3 of purified gas flow in purified gas introduction pipe line 2 consistent.Only a part of purified gas flows out in Methanol Wash Column 1, controls its flow to coordinate the design requirement amount of air lift regenerator 3.
Step 4) close nitrogen pipeline valve 8; Purified gas continues to flow in air lift regenerator 3.Cut off source nitrogen completely, air lift regenerator only utilizes purified gas to carry out work.
Step 5) when source nitrogen can continue enough the supply of nitrogen again in air lift regenerator 3, open nitrogen pipeline valve 8, close clean gas outlet and lead pouring 4; Enter normal productive process.Reach normal Production requirement, source nitrogen again can be supplied and continue enough nitrogen, for Mathanol regenerating in air lift regenerator 3; So the device designed by the present invention is closed.
Principle of the present invention is:
At identical temperature and uniform pressure, the solubility of hydrogen in methyl alcohol is less than the solubility of nitrogen in methyl alcohol.Composition due to purified gas is hydrogen 75%, nitrogen 24.8%, other 0.2%, compare with simple nitrogen, the content of hydrogen increases greatly.Therefore, the present invention utilizes purified gas as the gas stripping gas of air lift regenerator 3, is conducive to the dividing potential drop reducing purified gas in gas phase, improves the dividing potential drop of carbon dioxide gas, thus be conducive to the air lift of carbon dioxide and the regeneration of methyl alcohol.
At the same pressure, when temperature reduces, hydrogen and the nitrogen solubility in methyl alcohol all declines, nitrogen and hydrogen dividing potential drop in the gas phase all increases, that is: at the same pressure, when temperature reduces, purified gas and the same solubility in methyl alcohol of nitrogen all decline, and purified gas and the same dividing potential drop in the gas phase of nitrogen all increase.Therefore, the present invention utilizes purified gas as the gas stripping gas of air lift regenerator 3, is conducive to reducing carbon dioxide dividing potential drop in the gas phase, thus is conducive to the precipitation of carbon dioxide and the regeneration of methyl alcohol.
In actual production, the nitrogen used in air lift regenerator 3 is about 35 DEG C, and the rate of recovery of carbon dioxide is generally about 70%.Utilize the present invention, the purified gas imported from Methanol Wash Column 1 in air lift regenerator 3 is about 20 DEG C, and the rate of recovery of last carbon dioxide can reach 75%.
In actual production operation, if encounter various fault, and cannot ensure in air lift regenerator 3, provide lasting enough nitrogen, low-temperature rectisol step continuous firing cannot be ensured.In this case, often need air-separating plant to stop, overhaul; Also low-temperature rectisol step must be stopped equally simultaneously.Be in the synthetic ammonia factory of 400,000 tons/year in design output, air-separating plant is driven to normal condition after stopping again, and low-temperature rectisol step is driven equally to normal condition again, and front and back need at least 8 hours; During this, the economic loss only caused because reducing output is 800,000 yuan.
As can be seen here, adopt method of the present invention to the pipeline on improvement and installation between the Methanol Wash Column 1 in ammonia synthesis process and air lift regenerator 3 designed by the present invention.If meet the nitrogen supply (NS) fault needed for air lift regenerator 3 again, directly utilize purified gas to import in air lift regenerator 3, complete air lift Mathanol regenerating, ensure that low-temperature rectisol step is not stopped; Thus minimizing economic loss.
As can be seen here, the above, be only the specific embodiment of the present invention, it should be pointed out that any those of ordinary skill in the art are in the technical scope disclosed by the present invention, the change that can expect easily or replacement, all should be encompassed within protection scope of the present invention.
Claims (8)
1. the equipment of air lift regenerated methanol after low-temperature rectisol, be arranged between Methanol Wash Column (1) and air lift regenerator (3), it is characterized in that: clean gas outlet is set on the clean gas outlet pipeline at Methanol Wash Column (1) top and leads pouring (4); The downstream that described clean gas outlet leads pouring (4) connects purified gas introduction pipe line (2); Purified gas introduction pipe line (2) access gas stripping gas pipeline (6); Described gas stripping gas pipeline (6) one end passes into the bottom of air lift regenerator (3), and the other end connects source nitrogen.
2. the equipment of air lift regenerated methanol after low-temperature rectisol according to claim 1, is characterized in that: described purified gas introduction pipe line (2) is also provided with pressure-reducing valve (5).
3. the equipment of air lift regenerated methanol after low-temperature rectisol according to claim 1 and 2, is characterized in that: close source nitrogen one end of described gas stripping gas pipeline (6) is provided with nitrogen pipeline valve (8); The end of described gas stripping gas pipeline (6) near air lift regenerator (3) bottom is provided with gas stripping gas pipeline valve (7).
4. the equipment of air lift regenerated methanol after low-temperature rectisol according to claim 3, is characterized in that: the position of described purified gas introduction pipe line (2) access gas stripping gas pipeline (6) is between nitrogen pipeline valve (8) and air lift gas pipeline valve (7).
5. the equipment of air lift regenerated methanol after low-temperature rectisol according to claim 1, it is characterized in that: on the clean gas outlet pipeline at Methanol Wash Column (1) top, be no more than, 10 meters, described Methanol Wash Column (1) top and described clean gas outlet is set leads pouring (4).
6. the using method of the equipment of air lift regenerated methanol after above-mentioned low-temperature rectisol according to requirement arbitrary in Claims 1 to 5, is characterized in that, comprise the steps:
Step 1) source nitrogen be when cannot continue to provide enough nitrogen, open clean gas outlet and lead pouring (4), Methanol Wash Column (1) top has Partial cleansing gas to lead in pouring (4) inflow purified gas introduction pipe line (2) by clean gas outlet;
Step 2) regulate pressure-reducing valve (5), make the pressure of the purified gas flowed out in Methanol Wash Column (1) identical with the desorption pressures in air lift regenerator (3);
Step 3) regulate the gentle nitrogen flow carried needed for regenerator (3) of purified gas flow in purified gas introduction pipe line (2) consistent;
Step 4) close nitrogen pipeline valve (8); Purified gas continues to flow in air lift regenerator (3);
Step 5) when source nitrogen can continue enough the supply of nitrogen again in air lift regenerator (3), open nitrogen pipeline valve (8), close clean gas outlet and lead pouring (4); Enter normal productive process.
7. the using method of the equipment of air lift regenerated methanol after low-temperature rectisol according to claim 6, is characterized in that: described step 2) in, pressure-reducing valve (5) by the Pressure Drop of described purified gas to being less than 0.25MPa.
8. the using method of the equipment of air lift regenerated methanol after low-temperature rectisol according to claim 6, is characterized in that: described step 3) in, the purified gas flow in purified gas introduction pipe line (2) is 2000 ~ 3000m
3/ h.
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| CN201510242607.5A CN104857817A (en) | 2015-05-12 | 2015-05-12 | Low temperature methanol washing gas stripping regeneration methyl alcohol equipment and utilization method thereof |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510242607.5A CN104857817A (en) | 2015-05-12 | 2015-05-12 | Low temperature methanol washing gas stripping regeneration methyl alcohol equipment and utilization method thereof |
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| CN104857817A true CN104857817A (en) | 2015-08-26 |
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ID=53904243
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| CN201510242607.5A Pending CN104857817A (en) | 2015-05-12 | 2015-05-12 | Low temperature methanol washing gas stripping regeneration methyl alcohol equipment and utilization method thereof |
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| CN105344211A (en) * | 2015-12-02 | 2016-02-24 | 天津渤化永利化工股份有限公司 | Method for efficiently removing impurities in methanol washed in low-temperature methanol washing system |
| CN108014601A (en) * | 2016-11-04 | 2018-05-11 | 林德股份公司 | Method and apparatus for purification gas |
| CN110732150A (en) * | 2018-07-18 | 2020-01-31 | 中国石油化工股份有限公司 | Rectification adsorption purification process for waste methanol |
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Application publication date: 20150826 |