CN201665527U - One-through type isothermal methane-methanol depth purification device - Google Patents
One-through type isothermal methane-methanol depth purification device Download PDFInfo
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- CN201665527U CN201665527U CN2009200759204U CN200920075920U CN201665527U CN 201665527 U CN201665527 U CN 201665527U CN 2009200759204 U CN2009200759204 U CN 2009200759204U CN 200920075920 U CN200920075920 U CN 200920075920U CN 201665527 U CN201665527 U CN 201665527U
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Abstract
The utility model discloses a one-through type isothermal methane-methanol depth purification device which is arranged between a low-pressure cylinder and a high-pressure cylinder of a synthetic gas compressor. The one-through type isothermal methane-methanol depth purification device comprises at least one methylation reactor and a heat-insulated methylation reactor which are connected with each other in series. After being transformed and decarbonized, process gas coming from a gas generation working section enters the methylation reactor for methylation after being compressed by the low-pressure cylinder of the synthetic gas compressor, then enters the heat-insulated methylation reactor for methanation, and is finally sent out after methanation. The one-through type isothermal methane-methanol depth purification device is suitable for the synthetic gas depth purification process with coal, natural gas, acetylene tail gas, coal-generated synthetic oil tail gas and the like as raw materials to prepare synthesis ammonia; and the quality of purified gas can meet the requirement of ammonia synthesis catalysts. Meanwhile, with the advantages of high purification efficiency, strong adaptability, simple process, small investment, low energy consumption, simple operation, no pollution and the like, the one-through type isothermal methane-methanol depth purification device solves the problems of the present synthesis ammonia (synthesis gas) depth purification process and device, and leads the content of CO+CO2 in the synthetic gas to be less than 10ppmv.
Description
Technical field
The utility model belongs to gas sweetening and nitrogen fertilizer industry technical field, relate in particular to the two first deep purifying devices of through type isothermal one time, 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.
The utility model content
Technical problem to be solved in the utility model 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 deep purifying devices, 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.
Technical problem to be solved in the utility model can be achieved through the following technical solutions:
The two first deep purifying devices of through type isothermal, 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 utility model 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 utility model, temperature of reaction is controlled by the by-product saturated vapour pressure.
The utility model makes the next process gas of gas making workshop section behind conversion decarburization, remaining CO+CO
2Content between 0.5%～8%, by after the synthesic gas compressor low pressure (LP) cylinder compression, the process gas that forms pressure and be 5.0～8.0MPa enters the two first deep purifying devices of an isothermal, carry out methanolizing and methanation reaction successively after, obtain CO+CO
2Process gas after the following purification of content 10ppmv is sent into next workshop section's dry decontamination.
Its 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.Also can be undertaken by an isothermal methanolizing reactor and an adiabatic methanol reactor successively.
Behind the utility model process gas process isothermal methanolizing reactor, 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 utility model 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.
Owing to adopted technique scheme, the utility model 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 utility model 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 utility model 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 utility model not only can be realized 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 utility model, 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 utility model 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 utility model 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 utility model 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 utility model 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 the utility model ordinary production.
Further specify the utility model 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 utility model embodiment.
Fig. 2 is the schema of the two first advanced purification process of 2 through type isothermals of the utility model embodiment.
Fig. 3 is the schema of the two first advanced purification process of 3 through type isothermals of the utility model embodiment.
Embodiment
For technique means, creation characteristic that the utility model is realized, reach purpose and effect is easy to understand, below in conjunction with concrete diagram, further set forth the utility model.
Embodiment 1
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 utility model and principal character and advantage of the present utility model.The technician of the industry should understand; the utility model is not restricted to the described embodiments; that describes in the foregoing description and the specification sheets just illustrates principle of the present utility model; under the prerequisite that does not break away from the utility model spirit and scope; the utility model also has various changes and modifications, and these changes and improvements all fall in claimed the utility model scope.The claimed scope of the utility model is defined by appending claims and equivalent thereof.
Claims (5)
1. the device of the two first advanced purification process of through type isothermal, 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.
2. device as claimed in claim 1 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.
3. device as claimed in claim 1 is characterized in that, described methanolizing reactor is an isothermal methanolizing reactor.
4. device as claimed in claim 1 is characterized in that, described methanolizing reactor is the adiabatic methanol reactor.
5. device as claimed in claim 1 is characterized in that, described methanolizing reactor is formed by an isothermal methanolizing reactor and adiabatic methanol combination of reactors.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009200759204U CN201665527U (en) | 2009-08-06 | 2009-08-06 | One-through type isothermal methane-methanol depth purification device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009200759204U CN201665527U (en) | 2009-08-06 | 2009-08-06 | One-through type isothermal methane-methanol depth purification device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201665527U true CN201665527U (en) | 2010-12-08 |
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ID=43266483
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009200759204U Expired - Lifetime CN201665527U (en) | 2009-08-06 | 2009-08-06 | One-through type isothermal methane-methanol depth purification device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110482568A (en) * | 2019-08-12 | 2019-11-22 | 上海国际化建工程咨询有限公司 | A kind of by-product alkanol for medium and small nitrogen fertilizer factory to be transformed and the method and system of cold and hot joint purification |
-
2009
- 2009-08-06 CN CN2009200759204U patent/CN201665527U/en not_active Expired - Lifetime
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110482568A (en) * | 2019-08-12 | 2019-11-22 | 上海国际化建工程咨询有限公司 | A kind of by-product alkanol for medium and small nitrogen fertilizer factory to be transformed and the method and system of cold and hot joint purification |
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|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20101208 |