CN101659397A - Once-through isothermal methanol-methanation advanced purification process and device - Google Patents
Once-through isothermal methanol-methanation advanced purification process and device Download PDFInfo
- Publication number
- CN101659397A CN101659397A CN200910055999A CN200910055999A CN101659397A CN 101659397 A CN101659397 A CN 101659397A CN 200910055999 A CN200910055999 A CN 200910055999A CN 200910055999 A CN200910055999 A CN 200910055999A CN 101659397 A CN101659397 A CN 101659397A
- Authority
- CN
- China
- Prior art keywords
- gas
- isothermal
- methanolizing
- reactor
- purification process
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- 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
- Y02P20/10—Process efficiency
Abstract
The invention discloses a once-through isothermal methanol-methanation advanced purification process which ensures that process gas from gas producing working sections is changed, decarbonized, and compressed by a low-pressure cylinder of a synthesis gas compressor, then enters an isothermal methanol-methanation advanced purification device and is sequentially subject to methanolizing and methanation reactions to obtain the process gas with the content of CO plus CO2 less than 10ppmv, and the process gas is fed into the next working section for drying and purifying. The invention is suitable for a synthesis gas advanced purification process for preparing synthetic ammonia by taking coal, natural gas, acetylene tail gas and coal synthetic tail gas and the like as raw materials, enables thepurified gas to meet the requirements of ammonia synthetic catalysts, has the advantages of high purifying efficiency, strong adaptability, simple flow, less investment, low energy consumption, simpleoperation, no pollution and the like, solves the problems existing in the prior synthetic ammonia and synthetic gas advanced purification process and device and ensures that the content of the CO plus CO2 in the synthesis gas is less than 10ppmv. The invention also provides a device for realizing the once-through isothermal methanol-methanation advanced purification process.
Description
Technical field
The invention belongs to gas sweetening and nitrogen fertilizer industry technical field, relate in particular to two first advanced purification process of through type isothermal and device, be applicable to that with coal, natural gas, acetylene tail gas, coal system synthetic oil tail gas etc. be the synthetic gas deep purifying process of feedstock production synthetic ammonia, the purified gas quality satisfies the requirement of ammonia synthesis catalyst.
Background technology
Synthetic ammonia process is the basis of all nitrogen fertilizer industries, and Chinese rural economy is played very important effect.Ammonia synthesizing industry is again the industry of high energy consumption, even the synthetic ammonia technology is made improvements slightly, in industry promote will be positive to the energy-conservation generation of whole ammonia synthesizing industry effect.
Ammonia-synthesizing material gas must be purified hydrogen and nitrogen at present, if the CO remaining quantity is that 20ppmv will reduce ammonia synthesis reaction speed more than 10% in the syngas for synthetic ammonia.And with coal, natural gas, acetylene tail gas, coal system synthetic oil tail gas etc. be the synthetic gas of feedstock production synthetic ammonia behind conversion decarburization, contain 0.5%～8% CO+CO2, need remove.
A small amount of CO+CO in the existing syngas for synthetic ammonia
2Removal methods is a lot, has copper to wash purification process such as method, pure alkylation methods, pure alkylation methods, methanation method, liquid nitrogen washing, and relative merits are respectively arranged.
The copper method of washing can remove CO, CO remaining in the unstripped gas
2, be China's ammonia synthesizing industry a kind of main method of refining unstripped gas for a long time, very ripe in the application of China.Shortcomings such as but this method not only has the energy consumption height, hydrogen recovery rate is low, the raw material gas purifying degree is low, process cost is high, complex process, resistance drop is big, operation easier is big, and environmental pollution is serious, contain heavy metal copper, ammonia, carbon monoxide, carbonic acid gas etc. in the waste water, be unfavorable for environmental protection, copper is washed method and is progressively eliminated.
Adopt CO and CO2 in the methanation method removing process gas can simplify Production Flow Chart significantly, reduce and build and process cost, working cost is washed low than copper, and floor space is also washed few than copper.But in order to guarantee not overtemperature of methanation reaction temperature, advance the process gas carbon content of methanation workshop section and must strictly control, this has just proposed harsher requirement to conversion decarburization workshop section, and operating restraint is narrow; After oxycarbide all was converted into methane in addition, synthetic ammonia workshop section inert gas content height discharged large-mindedly, causes virgin gas consumption big, synthetic ammonia energy consumption height.
Liquid nitrogen washing needs a large amount of purity nitrogens as washing liq, therefore needs supporting air separation facility, it is generally acknowledged that liquid nitrogen washing purifies and low-temperature rectisol is supporting relatively to have superiority.
Alcohol alkylation methods, pure alkylation methods are to the wide adaptability of unstripped gas, requirement to conversion section is looser, and the oxycarbide in the unstripped gas is converted into useful product, when improving the business economic benefit, reduce the discharge quantity of synthetic ammonia, the ammonia-alcohol ratio regulation range is big, and production run is stable, simple to operate.At present, the pure alkylation methods of industrial use, pure alkylation methods all have characteristics separately, but also exist shortcoming, for example: press alcoholization, high pressure alcoholization and high pressure alkanisation in the pure alkylation methods right and wrong equipressure, though under high pressure help the generation of methyl alcohol and methane, CO and CO
2Gas need be compressed to high pressure, has not only increased the compressor power consumption, and has increased the danger of leaking; The medium and high pressure refining plant respectively with compressor serial flow back and forth, the flow process complexity, big to the compressor influence, be not suitable for the radial compressor flow process especially; The medium and high pressure purification process is not suitable for the low pressure ammonia synthesis technology, generally is only applicable to medium and small chemical fertilizer plant.The core of alcohol alkylation methods is to adopt smart desulfurization, methanolizing, three processes of methanation, and process gas is gone here and there between three processes back and forth, and the complicated resistance of flow process is big; The heating of employing electric-furnace-tube, the flow process complexity; Adopt the adiabatic methanol reactor, can not the by-product middle pressure steam, energy utilization efficiency is low, and wastes a large amount of water coolants; Per pass conversion is low, and energy-saving effect is poor; Generally be only applicable to medium and small chemical fertilizer plant.
No matter be pure alkylation methods, or pure alkylation methods, because of its alcohol/ammonia ratio scope that can reach very big (0.067～1.25 or 0.06～1.3), promptly the output of methyl alcohol can account for pure ammonia ultimate production 6～7% to 70～80% and can regulate, certainly will cause the waste of chemical plant installations production capacity and investment.When being voluminous methyl alcohol, cause the production capacity waste and the underload fallback of ammonia synthesis; During fecund synthetic ammonia, can cause the production capacity waste and the underload fallback of methanol device again.This is contrary with the design operation theory of modernized large scale chemical plant.
Summary of the invention
One of technical problem to be solved by this invention is to be purpose with the synthetic gas deep purifying, the gross investment of pursuing conversion decarburization and deep purifying is minimum, the total energy consumption of conversion decarburization and deep purifying is minimum, the comprehensive cost of methyl alcohol and ammonolysis product is minimum, and do not pursue high or low alcohol/ammonia ratio is purpose, and provide an a kind of through type isothermal two first advanced purification process, to be applicable to that with coal, natural gas, acetylene tail gas, coal system synthetic oil tail gas etc. be the synthetic gas deep purifying process of feedstock production synthetic ammonia, the purified gas quality satisfies the requirement of ammonia synthesis catalyst.Have the purification efficiency height simultaneously, adaptability is strong, flow process is simple, investment is little, energy consumption is low, advantage such as simple to operate, pollution-free, solve the problem that exists in present synthetic ammonia synthetic gas advanced purification process and the device, make CO+CO2 content in synthetic gas be lower than 10ppmv.
Two of technical problem to be solved by this invention provides the device of realizing the two first advanced purification process of an above-mentioned through type isothermal.
As the two first advanced purification process of a through type isothermal of first aspect present invention, make the next process gas of gas making workshop section behind conversion decarburization, after the compression of synthesic gas compressor low pressure (LP) cylinder, enter the two first deep purifying devices of an isothermal, after carrying out methanolizing and methanation reaction successively, obtain CO+CO
2Process gas after the following purification of content 10ppmv is sent into next workshop section's dry decontamination.
In the alleged technology of the present invention, the two first deep purifying devices of isothermal are arranged between the low pressure (LP) cylinder and high pressure cylinder of synthesic gas compressor.
In the alleged technology of the present invention, the process gas that gas making workshop section comes behind conversion decarburization, remaining CO+CO
2Content between 0.5%～8%.
The pressure that enters the process gas of the two first deep purifying devices of isothermal is 5.0～8.0MPa.
Described methanolizing reaction is when carbon content in the process gas that enters the two first deep purifying devices of isothermal is low, in order to shorten flow process, to simplify the operation, reduce investment, when unstripped gas carries out methanolizing, can in an isothermal methanolizing reactor or an adiabatic methanol reactor, carry out.
Described methanolizing reaction also can be undertaken by an isothermal methanolizing reactor and an adiabatic methanol reactor successively.
Behind the process gas process isothermal methanolizing reactor of the present invention, CO+CO
2Under catalyst action with H
2Reaction generates CH
3OH and H
2O, and emit a large amount of heat, heat is removed by oiler feed, presses saturation steam and separation of methanol in the by-product simultaneously, enters adiabatic methanol reactor reaction, CO+CO through the process gas behind the isothermal methanolizing reactor reaction
2Residual volume is also further isolated methyl alcohol less than 0.5%.
The present invention enters methanator through the reacted process gas of methanolizing and carries out methanation reaction, remaining CO+CO
2Be converted into methane, CO+CO
2Content drops to below the 10ppmv, sends after cooling divides water.
The alleged dry decontamination of the present invention adopts liquefied ammonia washing dry decontamination or molecular sieve drying to purify.
As the two first deep purifying devices of a through type isothermal of second aspect present invention, be arranged on the synthesic gas compressor low pressure (LP) cylinder, high pressure cylinder is intersegmental, it comprises a placed in-line at least one methanolizing reactor and an adiabatic methanol reactor mutually, the process gas that gas making workshop section comes is behind conversion decarburization, carry out methanolizing by entering the methanolizing reactor after the compression of synthesic gas compressor low pressure (LP) cylinder, then enter the adiabatic methanol reactor and carry out methanation reaction, be sent behind the methanation reaction.
Synthesic gas compressor of the present invention is a radial compressor, has low pressure (LP) cylinder and high pressure cylinder or multi-cylinder at least.
Described methanolizing reactor is isothermal methanolizing reactor or adiabatic methanol reactor or is formed by an isothermal methanolizing reactor and adiabatic methanol combination of reactors.
Press saturation steam in the isothermal methanolizing reactor by-product of the present invention, temperature of reaction is controlled by the by-product saturated vapour pressure.
Owing to adopted technique scheme, the present invention compared with prior art has following advantage:
1, allows the CO+CO of the next process gas of gas making through remnants about 0.5%～8% behind the conversion decarburization
2, with investment and the energy consumption that reduces conversion decarburization significantly.
2, the present invention all adopts common equipment to finish the target of synthetic gas deep purifying.
3, the two first deep purifying devices of isothermal of the present invention are pressed saturation steam in by-product methyl alcohol and the by-product when purifying synthetic gas, reduce cooling-water consumption significantly, are energy-efficient technology.
4, the present invention not only can realize the obnoxious flavour CO+CO with ammonia synthesis
2Be converted into methyl alcohol, and can reduce the content of synthesizing section inert component methane, methane content is low in the process gas after the methanation, and it is little to reach ammonia synthesis workshop section internal circulating load, and discharge quantity reduces, reaches the purpose of energy-saving and emission-reduction.
5, the two first deep purifying devices of isothermal of the present invention, the single device volume is little, and whole plant investment economizes, simple to operate;
6, the two first deep purifying devices of isothermal of the present invention adopt isothermal methanolizing reactor, for the adiabatic methanol reactor, fully phase out the use of circulator, and turndown ratio is bigger, and does not have the danger of overtemperature temperature runaway.
7, the two first deep purifying devices of isothermal of the present invention all adopt isothermal or adiabatic autothermic reactor, and the electric-furnace-tube well heater is used in cancellation.
8, the setting of adiabatic methanol reactor in the two first deep purifying devices of isothermal of the present invention can be with a spot of CO+CO in the process gas from isothermal methanolizing reactor
2Further be converted into methyl alcohol, reduce CO+CO
2Concentration, promptly reduce ammonia synthesis loop inert fraction CH4 content, guarantee not overtemperature temperature runaway not of methanator.
9, the methanator in the two first deep purifying devices of isothermal of the present invention can be with the CO+CO of trace
2Be converted into CH
4, CO+CO in the process gas that makes out
2Content is lower than 10ppmv, reaches the purpose of syngas for synthetic ammonia deep purifying;
10, three-waste free discharge during ordinary production of the present invention.
Further specify the present invention below in conjunction with the drawings and specific embodiments.
Description of drawings
Fig. 1 is the schema of the two first advanced purification process of 1 through type isothermals of the embodiment of the invention.
Fig. 2 is the schema of the two first advanced purification process of 2 through type isothermals of the embodiment of the invention.
Fig. 3 is the schema of the two first advanced purification process of 3 through type isothermals of the embodiment of the invention.
Embodiment
For technique means, creation characteristic that the present invention is realized, reach purpose and effect is easy to understand, below in conjunction with concrete diagram, further set forth the present invention.
This embodiment is applied on the new device, and its energy-saving effect is obvious.The two first deep purifying devices of the through type isothermal of this embodiment, comprise a synthesic gas compressor, this synthesic gas compressor is a radial compressor, have a low pressure (LP) cylinder 110 and a high pressure cylinder 120, also comprise a pair of first deep purifying device 300, this pair first deep purifying device 200 is in series by an isothermal methanolizing reactor R1, an adiabatic methanol reactor R2 and an adiabatic methanation reactor R3.
The process gas 1 that the conversion desulfurization and decarburization comes after compressed machine low pressure (LP) cylinder 110 compressions, enters under 5.0～8.0MPa pressure in two first deep purifying devices 300.This process gas 1 enters isothermal methanolizing reactor R1 after at first being preheated to 200～250 ℃ of temperature, presses saturation steam in the isothermal methanolizing reactor R1 by-product, and temperature of reaction is controlled by the by-product saturated vapour pressure.The process gas that goes out isothermal methanolizing reactor R1 enters adiabatic methanol reactor R2, remaining CO+CO behind recovery of heat and separation of methanol
2Further be converted into methyl alcohol.The CO+CO2 of remaining trace sends into adiabatic methanation reactor R3 in the process gas, go out that oxycarbide content is lower than 10ppmv in the process gas of adiabatic methanation reactor R3, after cooling divides water, send into downstream liquefied ammonia washing or molecular sieve drying refining plant 300 and continue a spot of moisture and CO in the removing process gas
2A spot of moisture and CO in the removing process gas
2After process gas by compressor high pressure cylinder 120 compression after, form and divide the ammonia ammino to grow up to be a useful person 400 after synthetic gas enters tower, grow up to be a useful person a part of gas of 400 of ammino is delivered to synthetic ammonia workshop section, another part forms circulation gas and sends into compressor high pressure cylinder 120, tail gas is sent into hydrogen withdrawer 500 recover hydrogen, and the hydrogen of recovery mixes with process gas 1.
Isothermal methanolizing reactor R1 in two first deep purifying devices 300 feeds in the de-salted water by-product and presses saturation steam, and adiabatic methanol reactor R2 and adiabatic methanation reactor R3 can feed in the de-salted water by-product and press superheated vapour.During adopting and feed, the heating and cooling of two first deep purifying devices 300 press superheated vapour and water coolant to carry out.
The composition of the process gas 1 behind the desulfurization and decarburization is (V%): CO 4～8, CO
20.1～0.3, H2 63～71, CH
40.1～1, Ar 0.1～1, N2 18～20.Methyl alcohol by-product saturation steam amount per ton is:＞0.8t/t (2.5MPaG, 226 ℃)
Embodiment 2:
If total carbon content reduces in the desulfurization and decarburization unstripped gas, can adopt following examples 2, reduce investment.The just two first deep purifying devices 200 of this embodiment are different with embodiment 1, are to be in series by an isothermal methanolizing reactor R1 and an adiabatic methanation reactor R3.Rest part is identical with embodiment 1.
The process gas 1 that the conversion desulfurization and decarburization comes after compressed machine low pressure (LP) cylinder 110 compressions, enters under 5.0～8.0MPa pressure in two first deep purifying devices 300.This process gas 1 enters isothermal methanolizing reactor R1 after at first being preheated to 200～250 ℃ of temperature, presses saturation steam in the isothermal methanolizing reactor R1 by-product, and temperature of reaction is controlled by the by-product saturated vapour pressure.The process gas that goes out isothermal methanolizing reactor R1 is behind recovery of heat and separation of methanol, send into adiabatic methanation reactor R3, the process gas oxycarbide content that goes out methanator R3 is lower than 10ppmv, after cooling divides water, send into downstream liquefied ammonia washing or molecular sieve drying refining plant 300 and continue a spot of moisture and CO2 in the removing process gas.A spot of moisture and CO in the removing process gas
2After process gas by compressor high pressure cylinder 120 compression after, form and divide the ammonia ammino to grow up to be a useful person 400 after synthetic gas enters tower, grow up to be a useful person a part of gas of 400 of ammino is delivered to synthetic ammonia workshop section, another part forms circulation gas and sends into compressor high pressure cylinder 120, tail gas is sent into hydrogen withdrawer 500 recover hydrogen, and the hydrogen of recovery mixes with process gas 1.
Isothermal methanolizing reactor R1 in two first deep purifying devices 300 feeds in the de-salted water by-product and presses saturation steam, and adiabatic methanation reactor R3 can feed in the de-salted water by-product and press superheated vapour.During adopting and feed, the heating and cooling of two first deep purifying devices 300 press superheated vapour and water coolant to carry out.
The composition of the process gas 1 behind the desulfurization and decarburization is (V%): CO 2～4, CO
20.1～0.3, H2 66～72, CH
40.1～1, Ar 0.1～1, N2 21～23.Methyl alcohol by-product saturation steam amount per ton is:＞0.9t/t (2.5MPaG, 226 ℃)
Embodiment 3:
If total carbon content further reduces in the desulfurization and decarburization unstripped gas, can adopt following examples 3, further reduce investment; It is obvious to be applied on the device for modifying energy-saving and production-increase effect.The just two first deep purifying devices 200 of this embodiment are different with embodiment 1, are to be in series by an adiabatic methanol reactor R2 and an adiabatic methanation reactor R3.Rest part is identical with embodiment 1.
The process gas 1 that the conversion desulfurization and decarburization comes after compressed machine low pressure (LP) cylinder 110 compressions, enters under 5.0～8.0MPa pressure in two first deep purifying devices 300.This process gas 1 enters adiabatic methanol reactor R2, remaining CO+CO after at first being preheated to 200～230 ℃ of temperature
2Further be converted into methyl alcohol.The process gas that goes out adiabatic methanol reactor R2 is behind recovery of heat and separation of methanol, send into adiabatic methanation reactor R3, the process gas oxycarbide content that goes out methanator R3 is lower than 10ppmv, after cooling divides water, send into downstream liquefied ammonia washing or molecular sieve drying refining plant 300 and continue a spot of moisture and CO2 in the removing process gas.A spot of moisture and CO in the removing process gas
2After process gas by compressor high pressure cylinder 120 compression after, form and divide the ammonia ammino to grow up to be a useful person 400 after synthetic gas enters tower, grow up to be a useful person a part of gas of 400 of ammino is delivered to synthetic ammonia workshop section, another part forms circulation gas and sends into compressor high pressure cylinder 120, tail gas is sent into hydrogen withdrawer 500 recover hydrogen, and the hydrogen of recovery mixes with process gas 1.
Adiabatic methanol reactor R2 in two first deep purifying devices 300 and adiabatic methanation reactor R3 can feed in the de-salted water by-product and press superheated vapour.During adopting and feed, the heating and cooling of two first deep purifying devices 300 press superheated vapour and water coolant to carry out.
The composition of the process gas 1 behind the desulfurization and decarburization is (V%): CO 1～2, CO
20.1～0.3, H2 69～73, CH
40.1～1, Ar 0.1～1, N2 23～24.
More than show and described ultimate principle of the present invention and principal character and advantage of the present invention.The technician of the industry should understand; the present invention is not restricted to the described embodiments; that describes in the foregoing description and the specification sheets just illustrates principle of the present invention; without departing from the spirit and scope of the present invention; the present invention also has various changes and modifications, and these changes and improvements all fall in the claimed scope of the invention.The claimed scope of the present invention is defined by appending claims and equivalent thereof.
Claims (17)
1. two first advanced purification process of through type isothermal, make the next process gas of gas making workshop section behind conversion decarburization, after the compression of synthesic gas compressor low pressure (LP) cylinder, enter the two first deep purifying devices of isothermal of a synthetic ammonia synthetic gas, after carrying out methanolizing and methanation reaction successively, obtain CO+CO
2Process gas after the following purification of content 10ppmv is sent into next workshop section's dry decontamination.
2. the two first advanced purification process of a through type isothermal as claimed in claim 1 is characterized in that, the two first deep purifying devices of described isothermal are arranged between the low pressure (LP) cylinder and high pressure cylinder of synthesic gas compressor.
3. the two first advanced purification process of a through type isothermal as claimed in claim 1 is characterized in that, the process gas that described gas making workshop section comes behind conversion decarburization, remaining CO+CO
2Content between 0.5%～8%.
4. the two first advanced purification process of a through type isothermal as claimed in claim 1 is characterized in that, the pressure of the process gas of the described two first deep purifying devices of isothermal that enter the synthetic ammonia synthetic gas is 5.0～8.0MPa.
5. the two first advanced purification process of a through type isothermal as claimed in claim 1 is characterized in that described methanolizing is reflected in the isothermal methanolizing reactor and carries out.
6. the two first advanced purification process of a through type isothermal as claimed in claim 1 is characterized in that described methanolizing is reflected in the adiabatic methanol reactor and carries out.
7. the two first advanced purification process of a through type isothermal as claimed in claim 1 is characterized in that, described methanolizing reaction is undertaken by an isothermal methanolizing reactor and an adiabatic methanol reactor successively.
8. the two first advanced purification process of a through type isothermal as claimed in claim 1 is characterized in that, behind the described process gas process isothermal methanolizing reactor, and CO+CO
2Under catalyst action with H
2Reaction generates CH
3OH and H
2O, and emit a large amount of heat, heat is removed by oiler feed, presses saturation steam and separation of methanol in the by-product simultaneously, enters adiabatic methanol reactor reaction, CO+CO through the process gas behind the isothermal methanolizing reactor reaction
2Residual volume is also further isolated methyl alcohol less than 0.5%.
9. the two first advanced purification process of a through type isothermal as claimed in claim 1 is characterized in that, enter methanator through the reacted process gas of methanolizing and carry out methanation reaction, remaining CO+CO
2Be converted into methane, CO+CO
2Content drops to below the 10ppmv, sends after cooling divides water.
10. the two first advanced purification process of a through type isothermal as claimed in claim 1 is characterized in that, described dry decontamination adopts liquefied ammonia washing dry decontamination or molecular sieve drying to purify.
11, the two first advanced purification process of a through type isothermal as claimed in claim 1, it is characterized in that, enter the two first deep purifying devices of isothermal of a synthetic ammonia synthetic gas, carry out methanolizing and methanation reaction more successively after at first being preheated to 200～230 ℃ of temperature.
12. device of realizing the two first advanced purification process of the described through type isothermal of claim 1, it is characterized in that, be arranged on the synthesic gas compressor low pressure (LP) cylinder, high pressure cylinder is intersegmental, this device comprises a placed in-line at least one methanolizing reactor and an adiabatic methanol reactor mutually, the process gas that gas making workshop section comes is behind conversion decarburization, carry out methanolizing by entering the methanolizing reactor after the compression of synthesic gas compressor low pressure (LP) cylinder, then enter the adiabatic methanol reactor and carry out methanation reaction, be sent behind the methanation reaction.
13. device as claimed in claim 12 is characterized in that, described synthesic gas compressor is a radial compressor, has low pressure (LP) cylinder and high pressure cylinder or multi-cylinder at least.
14. device as claimed in claim 12 is characterized in that, described methanolizing reactor is an isothermal methanolizing reactor.
15. device as claimed in claim 12 is characterized in that, described methanolizing reactor is the adiabatic methanol reactor.
16. device as claimed in claim 12 is characterized in that, described methanolizing reactor is formed by an isothermal methanolizing reactor and adiabatic methanol combination of reactors.
17. device as claimed in claim 14 is characterized in that, presses saturation steam in the described isothermal methanolizing reactor by-product, temperature of reaction is controlled by the by-product saturated vapour pressure.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910055999A CN101659397A (en) | 2009-08-06 | 2009-08-06 | Once-through isothermal methanol-methanation advanced purification process and device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910055999A CN101659397A (en) | 2009-08-06 | 2009-08-06 | Once-through isothermal methanol-methanation advanced purification process and device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101659397A true CN101659397A (en) | 2010-03-03 |
Family
ID=41787683
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200910055999A Pending CN101659397A (en) | 2009-08-06 | 2009-08-06 | Once-through isothermal methanol-methanation advanced purification process and device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101659397A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105947981A (en) * | 2016-05-06 | 2016-09-21 | 南京昊安科技工程有限公司 | High pressure water-cooling phase change heat transfer methanolization and methanation refining technology |
| CN106865568A (en) * | 2017-04-14 | 2017-06-20 | 山西兰花科技创业股份有限公司 | One kind is using regenerating molecular sieve gas to double first catalyzer temperature-elevating systems and its technique |
| CN109279573A (en) * | 2018-09-30 | 2019-01-29 | 中石化宁波工程有限公司 | A kind of isothermal conversion process of mating coal water slurry gasification |
-
2009
- 2009-08-06 CN CN200910055999A patent/CN101659397A/en active Pending
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105947981A (en) * | 2016-05-06 | 2016-09-21 | 南京昊安科技工程有限公司 | High pressure water-cooling phase change heat transfer methanolization and methanation refining technology |
| CN105947981B (en) * | 2016-05-06 | 2018-06-15 | 南京昊安科技工程有限公司 | The phase transformation of high pressure water cooling moves hot alcohol alkanisation process for refining |
| CN106865568A (en) * | 2017-04-14 | 2017-06-20 | 山西兰花科技创业股份有限公司 | One kind is using regenerating molecular sieve gas to double first catalyzer temperature-elevating systems and its technique |
| CN106865568B (en) * | 2017-04-14 | 2023-08-29 | 山西兰花科技创业股份有限公司 | System and process for heating double-methyl catalyst by using molecular sieve regenerated gas |
| CN109279573A (en) * | 2018-09-30 | 2019-01-29 | 中石化宁波工程有限公司 | A kind of isothermal conversion process of mating coal water slurry gasification |
| CN109279573B (en) * | 2018-09-30 | 2022-03-22 | 中石化宁波工程有限公司 | Isothermal transformation process matched with coal water slurry gasification |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102585951B (en) | Process for co-production of liquefied synthesis gas, pure hydrogen and methanol from coke-oven gas | |
| CN100526273C (en) | Method for integral production of liquid ammonia and methanol and/or dimethyl ether by using coke oven gas as raw material | |
| CN101544539B (en) | Method for producing polymer grade ethylene glycol and co-producing methyl glycolate | |
| CN101293812A (en) | Technique for joint production of methanol and natural gas with methyl hydride containing synthesis gas | |
| CN102517108A (en) | Technology for preparing liquefied natural gas and liquid ammonia by using coke oven gas | |
| CN101362973B (en) | Technique for preparing mixed fuel of hydrogen and dimethyl ether from methanol | |
| CN101550052B (en) | Process for producing methanol and coproducing methane by using synthesis gas containing methane | |
| CN102329670B (en) | Process for preparing synthesis gas from coke-oven gas | |
| CN102899112B (en) | Method and device for producing synthetic natural gas | |
| CN103131490A (en) | Technology of coke oven gas for methane production | |
| WO2014000503A1 (en) | Method for preparing liquid hydrocarbon product from biomass-produced synthetic gas | |
| CN104229831A (en) | Process for preparing synthesis ammonia from synthesis gas and co-producing ethylene glycol | |
| CN102876411B (en) | Method and device for producing synthetic natural gas | |
| CN103194286A (en) | Methanation method for synthesizing substitute natural gas by using industrial hydrocarbon exhaust gas | |
| CN102676251B (en) | Process for preparing methane by utilizing coke oven gas | |
| CN101659397A (en) | Once-through isothermal methanol-methanation advanced purification process and device | |
| CN102746870B (en) | FT synthesis technology | |
| CN202297421U (en) | Device for producing ethylene glycol by using metallurgical tail gas | |
| CN201665527U (en) | One-through type isothermal methane-methanol depth purification device | |
| CN201525833U (en) | Insulated methanation assembly for producing synthetic natural gas | |
| CN103013598B (en) | Method and device for producing synthesized natural gas | |
| CN100596293C (en) | Stage associating process for producing methanol and ammonia using coal and coke oven gas as material | |
| CN104513679A (en) | New technology for preparing natural gas through coke-oven gas methanation | |
| CN102219679B (en) | Method for producing oxalic acid ester through CO gas phase coupling | |
| CN108707064B (en) | Production method for co-producing dimethyl ether by using blast furnace gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C12 | Rejection of a patent application after its publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20100303 |