CN109384647A - A kind of transformation methanolizing integrated production equipment and method - Google Patents
A kind of transformation methanolizing integrated production equipment and method Download PDFInfo
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- CN109384647A CN109384647A CN201811250264.7A CN201811250264A CN109384647A CN 109384647 A CN109384647 A CN 109384647A CN 201811250264 A CN201811250264 A CN 201811250264A CN 109384647 A CN109384647 A CN 109384647A
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Abstract
The invention discloses a kind of transformation methanolizing integrated production equipment and methods, belong to synthesizing methanol and technical field of coal chemical industry.Mainly it is made of equipment such as change furnace, methyl alcohol synthetic reactor, gas-liquid separator and more heat exchanger series connection.Crude synthesis gas from upstream initially enters low-pressure steam generator and adjusts liquid to steam ratio, realize steam consumption with react after methanol content in process gas optimum balance.Reaction heat is taken away using water shifting heat formula isothermal reactor, reaction hot(test)-spot temperature is reduced, forward reaction is pushed to carry out, reduce the choice requirement of equipment and pipeline.Conversion reaction and methanol synthesis reaction are subjected to organic combination, it solves the problems, such as " malaria " existing for conventional process flow, synthesis gas needs not move through acid gas removal unit before entering methyl alcohol synthetic reactor, but it is directly entered transformation methanolizing process units, with applied widely, process is short, small investment, the features such as low energy consumption, and heating efficiency is high.
Description
Technical field
The invention belongs to synthesizing methanols and technical field of coal chemical industry, and in particular to a kind of transformation methanolizing integration production dress
It sets and method.
Background technique
Methanol is the basis of extremely important Organic Chemicals, is the basic product of C-1 chemistry, mainly for the production of
The downstream product such as alkene, formaldehyde, dimethyl ether and acetic acid.It is simultaneously also clean efficient civilian and vehicle liquid fuel and a new generation
The starting material of derived energy chemical.In recent years, China creates the large-sized methanol plant mainly specific gravity based on coal head, in aggregated capacity
Rapid development, it is contemplated that China's methanol production capacity in 2025 is 120,000,000 tons, and market has openings is up to 20,000,000 tons or so.
Methanol industry starts from early 20th century, original adoption zinc chromia catalyst, and 360~400 DEG C of reaction temperature, pressure limit is
Although 19.6~1294MPa, high-pressure process have more than 70 years history, but since raw material and power consumption are big, and reaction temperature is high, generate
The organic impurity content of crude carbinol is high, and invests greatly, and therefore, development is restricted.Britain's Imperial Chemical Industries work in 1966
After industry company (ICI) successfully develops Cu-Zn-Al catalyst, ICI low pressure methanol synthesis technique, Germany Lu Qigong in 1971 are released
It takes charge of (Lurgi) and successfully releases Lurgi low pressure methanol synthesis technique, both techniques are large-scale low pressure first most widely used at present
Alcohol synthesis technology.
Existing ammonia from coal technique mainly includes the coal gasification of front end and the methanol-fueled CLC of rear end.Coal gasification is according to feed coal
Characteristic can choose a variety of gasification process；And existing methanol synthesis technology is all to convert high-temperature crude synthesis gas instead by CO
H should be adjusted2With the ratio of CO, so that its reaction modulus requirement for meeting methanol-fueled CLC, progress is sour after being cooled to 40 DEG C or less
It is removed under property gas low temperature, carries out methanol synthesis reaction after being then heated to high temperature again.The temperature of entire process flow layout
Gradient is unreasonable, there are problems that " malaria ", and CO converter unit has a large amount of low temperature process condensate liquids to be discharged, and needs using steam vapour
Processing is proposed, causes full-flow process long, heat exchange equipment is relatively more, and investment is big, and operating cost is high.
Summary of the invention
It is an object of the invention to be directed to the problems of existing ammonia from coal technique whole process, to reduce ammonia from coal
The construction investment of project and operation energy consumption improve the economy of system, provide a kind of transformation methanolizing integral manufacturing technique,
Mainly it is made of equipment such as change furnace, methyl alcohol synthetic reactor, gas-liquid separator and more heat exchanger series connection.By conversion reaction and first
Alcohol synthesis reaction carries out organic combination, solves the problems, such as " malaria " existing for conventional process flow, and synthesis gas is entering methanol
Acid gas removal unit is needed not move through before synthetic tower, but is directly entered transformation methanolizing process units, has and is applicable in model
Enclose wide, the features such as process is short, and small investment, low energy consumption, and heating efficiency is high.
The purpose of the present invention can be achieved through the following technical solutions:
A kind of transformation methanolizing integrated production equipment, the device include low-pressure steam generator, crude synthesis gas separator,
Synthesize hot-air heater, detoxification slot, change furnace, desulfurization reactor, methyl alcohol synthetic reactor, the crude synthesis gas from upstream coal gasification apparatus
Pipeline is connected with the input terminal of low-pressure steam generator, and low-pressure steam generator is heated by crude synthesis gas separator and synthesis gas
Device is connected, and the synthesis hot-air heater at the top of detoxification slot and change furnace by being connected；The transformation furnace bottom output end is logical
It crosses synthesis hot-air heater to be connected with desulfurization reactor bottom, output channel and methanol-fueled CLC top of tower phase at the top of desulfurization reactor
Even, after methyl alcohol synthetic reactor outlet at bottom rich methanol technique feed channel passes sequentially through circulating gas heater and water cooler, into methanol
The bottom output liquid phase of separator, methanol separator is that crude carbinol product sends to out-of-bounds rectifier unit；Gas at the top of methanol separator
Mutually a part is sent to out-of-bounds as periodic off-gases, and another part successively after recycle gas compressor and circulating gas heater and is come
It is connected from desulfurization reactor top exit technique feed channel, methyl alcohol synthetic reactor is entered after mixing.
In technical solution of the present invention: the vapor uptake of change furnace and methyl alcohol synthetic reactor is connected with drum respectively, drum
Boiler feedwater down-comer is connected with change furnace and methyl alcohol synthetic reactor respectively.
In technical solution of the present invention: drum is provided with medium-pressure boiler feed supply pipeline and saturated vapor output is out-of-bounds managed
Road.
In technical solution of the present invention: the internals of methanol separator are efficiently divided using wire mesh demister, centrifugal or vane type
From structure.
It is a kind of to realize transformation methanolizing integrated production method using above-mentioned apparatus, method includes the following steps:
(1) crude synthesis gas from coal gasification unit is entered after low-pressure steam generator cooling and enters crude synthesis gas separation
Device isolates high temperature condensate liquid and returns to gasification, and gas phase, which enters after synthesis hot-air heater heating, removes impurity into detoxification slot, enters
Change furnace carries out the hydrogen-carbon ratio that CO conversion reaction adjusts process gas, obtains high temperature shift gas；
(2) high temperature shift gas enters synthesis hot-air heater, enters desulfurization reactor after being cooled and removes H in process gas2S etc.
Harmful substance, then be mixed into methyl alcohol synthetic reactor with the circulating air from recycle gas compressor and generate methanol；
(3) methyl alcohol synthetic reactor exit gas enters methanol separator, liquid after entering circulating gas heater and water cooler cooling
It is mutually that crude carbinol product goes rectification cell to refine, gas phase fixed gas a part is as periodic off-gases, and another part is by circulation air pressure
After the pressurization of contracting machine, methyl alcohol synthetic reactor is mixed into the process gas from desulfurization reactor after circulating gas heater heats up.
In the above method: step (1) is introduced into low-pressure steam generator pair from the crude synthesis gas of upstream coal gasification unit
Low-pressure saturated steam is produced, to control the liquid to steam ratio of crude synthesis gas, entering after being cooled in gas-liquid two crude synthesis gas is thick
It synthesizes gas separating device and carries out gas-liquid separation, liquid phase is that high temperature condensate liquid returns to gasification, and the resulting process gas of gas phase removes detoxification slot, slightly
The liquid to steam ratio of synthesis gas controls between 0.1~0.6.
In the above method: the process gas temperature into change furnace controls between 220~280 DEG C, and change furnace is isothermal
Reactor, operation temperature are controlled at 240~350 DEG C.
In the above method: the process gas temperature into methyl alcohol synthetic reactor controls the methanol-fueled CLC between 200~250 DEG C
Tower is isothermal reactor, and operation temperature is controlled at 220~320 DEG C.
In the above method: the CO transformation of change furnace and the methanol synthesis reaction heat of methyl alcohol synthetic reactor are moved back by boiler water vapor
Out, by-product saturated vapor sends to steam pipe network by drum, and the pressure of by-product saturated vapor is 2.0~4.5MPa.
In the above method: entering drum from medium-pressure boiler water out-of-bounds, the boiler water from drum is divided into two strands: one stock-traders' know-hows
The down-comer recycling reaction heat connecting with change furnace is crossed, another stock-traders' know-how crosses the down-comer recycling first connecting with methyl alcohol synthetic reactor
Alcohol reaction heat；Reaction heat is removed by boiler water byproduct steam, gained saturation pressure steam enters vapour by respective tedge respectively
It is sent to out-of-bounds after packet mixing.
Beneficial effects of the present invention:
A kind of transformation methanolizing integral manufacturing technique of the present invention, the crude synthesis gas from upstream initially enters low
Press steam generator to adjust liquid to steam ratio, realize steam consumption with react after methanol content in process gas optimum balance.Using
Controllable water shifting heat formula isothermal reactor takes away reaction heat, reduces reaction hot(test)-spot temperature, forward reaction is pushed to carry out, reduce equipment and
The choice requirement of pipeline.Crude synthesis gas from upstream coal gasification does not need after being cooled to 40 DEG C or less after conversion reaction
The CO in synthesis gas is removed into sour gas unit2And H2The impurity such as S, but directly adopt conversion reaction and methanol-fueled CLC skill
Art carries out organic combination, has that process flow is short, production energy consumption is low, and small investment, operating condition are controllable, energy utilization efficiency height etc.
Feature.
Detailed description of the invention
Fig. 1 is process flow diagram of the invention.
In figure: 1- low-pressure steam generator, 2- crude synthesis gas separator, 3- synthesize hot-air heater, 4- detoxification slot, 5- transformation
Furnace, 6- desulfurization reactor, 7- methyl alcohol synthetic reactor, 8- circulating gas heater, 9- water cooler, 10- methanol separator, 11- circulating air
Compressor, 12- drum.
Specific embodiment
Below with reference to embodiment, the present invention will be further described, and but the scope of the present invention is not limited thereto:
A kind of transformation methanolizing integrated production equipment, including low-pressure steam generator (1), crude synthesis gas separator (2),
Synthesize hot-air heater (3), detoxification slot (4), change furnace (5), desulfurization reactor (6), methyl alcohol synthetic reactor (7), circulating gas heater
(8), water cooler (9), methanol separator (10), recycle gas compressor (11) and drum (12) and its pipeline being connected are constituted.Come
It is connected from the crude synthesis gas pipeline of upstream coal gasification apparatus with the input terminal of low-pressure steam generator (1), low-pressure steam generator
(1) crude synthesis gas exported is connected with crude synthesis gas separator (2), crude synthesis gas separator (2) top gas phase pipeline and synthesis
Hot-air heater (3) is connected, and synthesis hot-air heater (3) outlet process gas is connected after being heated with detoxification slot (4) bottom, detoxification slot
(4) it is connected at the top of the purified synthesis gas pipeline in top and change furnace (5).Change furnace (5) bottom output end and synthesis gas heat
Device (3) is connected, and the technique feed channel after being cooled is connected with desulfurization reactor (6) bottom, efferent duct at the top of desulfurization reactor (6)
It is connected at the top of road and methyl alcohol synthetic reactor (7), methyl alcohol synthetic reactor (7) outlet at bottom rich methanol technique feed channel passes sequentially through circulating air
After heater (8) and water cooler (9), into methanol separator (10), the bottom output liquid phase of methanol separator (10) is thick first
Alcohol product sends to out-of-bounds rectifier unit.Methanol separator (10) top gas phase a part is sent to out-of-bounds as periodic off-gases, and in addition one
Recycle gas compressor (11) are successively passed through in part, and circulating gas heater (8) is afterwards and from desulfurization reactor top exit process gas
Pipeline is connected, and enters methyl alcohol synthetic reactor (7) after mixing.The vapor uptake of change furnace (5) and methyl alcohol synthetic reactor (7) respectively with vapour
It wraps (12) to be connected, the boiler feedwater down-comer of drum (12) is connected with change furnace (5) and methyl alcohol synthetic reactor (7) respectively.Drum
(12) medium-pressure boiler feed supply pipeline and saturated vapor output out-of-bounds pipeline are provided with.
A method of transformation methanolizing integration, which is carried out, using above-mentioned apparatus produces, the specific steps are as follows:
Embodiment 1
22400Nm from coal gasification unit3/ h synthesis gas, temperature are 245 DEG C, pressure 6.25MPa, composition
It (mol%) is CO:17.2%, H2: 14.2%, CO2: 9.4%, CH4: 0.25%, N2: 0.1%, AR:0.055%, into low pressure
After steam generator is cooled to 170 DEG C, into crude synthesis gas separator, isolates 9311kg/h high temperature condensate liquid and returns to gasification,
The water-gas ratio of synthesis gas is reduced to 0.2 by 1.42, and acquisition gas phase flow rate is 10837Nm3/ h, temperature are 170 DEG C and enter synthesis gas
Heater enters detoxification slot after being warming up to 220 DEG C and removes impurity, subsequently enters change furnace and carries out CO conversion reaction adjusting process gas
Hydrogen-carbon ratio；260 DEG C of high temperature shift gas enter synthesis hot-air heater, and desulfurization reactor is entered after being cooled to 211 DEG C and removes work
H in skill gas2The harmful substances such as S, then with the circulating air temperature from recycle gas compressor be 230 DEG C, flow 29098Nm3/ h is mixed
Enter methyl alcohol synthetic reactor after being bonded to 223 DEG C and generates methanol.Methyl alcohol synthetic reactor Outlet Gas Temperature is 245 DEG C, and flow is
36557Nm3/ h enters circulating gas heater and water cooler is cooled to 40 DEG C and enters methanol separator, and liquid phase obtains 3324kg/h,
Purity is that the crude carbinol product of 70.6% (mol) goes rectification cell to refine, and gas phase fixed gas a part is as periodic off-gases, another portion
Lease making cross recycle gas compressor pressurization after, after circulating gas heater is warming up to 230 DEG C with the technique from desulfurization reactor
Gas is mixed into methyl alcohol synthetic reactor.CO transformation and methanol synthesis reaction heat are moved back out by boiler water vapor, by-product 2310kg/h's
Saturated vapor (pressure 2.5MPa, temperature are 224 DEG C), sends to steam pipe network by drum.
Embodiment 2
22400Nm from coal gasification unit3/ h synthesis gas, temperature are 245 DEG C, pressure 6.25MPa, composition
It (mol%) is CO:17.2%, H2: 14.2%, CO2: 9.4%, CH4: 0.25%, N2: 0.1%, AR:0.055%, into low pressure
After steam generator is cooled to 152 DEG C, into crude synthesis gas separator, isolates 9822kg/h high temperature condensate liquid and returns to gasification,
The water-gas ratio of synthesis gas is reduced to 0.1 by 1.42, and acquisition gas phase flow rate is 10200Nm3/ h, temperature are 152 DEG C and enter synthesis gas
Heater enters detoxification slot after being warming up to 220 DEG C and removes impurity, subsequently enters change furnace and carries out CO conversion reaction adjusting process gas
Hydrogen-carbon ratio；240 DEG C of high temperature shift gas enter synthesis hot-air heater, and desulfurization reactor is entered after being cooled to 173 DEG C and removes work
H in skill gas2The harmful substances such as S, then with the circulating air temperature from recycle gas compressor be 212 DEG C, flow 21991Nm3/ h is mixed
Enter methyl alcohol synthetic reactor after being bonded to 200 DEG C and generates methanol.Methyl alcohol synthetic reactor Outlet Gas Temperature is 220 DEG C, and flow is
28241Nm3/ h enters circulating gas heater and water cooler is cooled to 40 DEG C and enters methanol separator, and liquid phase obtains 3629kg/h,
Purity is that the crude carbinol product of 74.7% (mol) goes rectification cell to refine, and gas phase fixed gas a part is as periodic off-gases, another portion
Lease making cross recycle gas compressor pressurization after, after circulating gas heater is warming up to 212 DEG C with the technique from desulfurization reactor
Gas is mixed into methyl alcohol synthetic reactor.CO transformation and methanol synthesis reaction heat are moved back out by boiler water vapor, by-product 2760kg/h's
Saturated vapor (pressure 2.5MPa, temperature are 224 DEG C), sends to steam pipe network by drum.
Embodiment 3
22400Nm from coal gasification unit3/ h synthesis gas, temperature are 245 DEG C, pressure 6.25MPa, composition
It (mol%) is CO:17.2%, H2: 14.2%, CO2: 9.4%, CH4: 0.25%, N2: 0.1%, AR:0.055%, into low pressure
After steam generator is cooled to 152 DEG C, into crude synthesis gas separator, isolates 6115kg/h high temperature condensate liquid and returns to gasification,
The water-gas ratio of synthesis gas is reduced to 0.6 by 1.42, and acquisition gas phase flow rate is 14807Nm3/ h, temperature are 214 DEG C and enter synthesis gas
Heater enters detoxification slot after being warming up to 280 DEG C and removes impurity, subsequently enters change furnace and carries out CO conversion reaction adjusting process gas
Hydrogen-carbon ratio；350 DEG C of high temperature shift gas enter synthesis hot-air heater, and desulfurization reactor is entered after being cooled to 286 DEG C and removes work
H in skill gas2The harmful substances such as S, then with the circulating air temperature from recycle gas compressor be 242 DEG C, flow 56203Nm3/ h is mixed
Enter methyl alcohol synthetic reactor after being bonded to 250 DEG C and generates methanol.Methyl alcohol synthetic reactor Outlet Gas Temperature is 320 DEG C, and flow is
70045Nm3/ h enters circulating gas heater and water cooler is cooled to 40 DEG C and enters methanol separator, and liquid phase obtains 3450kg/h,
Purity is that the crude carbinol product of 11.5% (mol) goes rectification cell to refine, and gas phase fixed gas a part is as periodic off-gases, another portion
Lease making cross recycle gas compressor pressurization after, after circulating gas heater is warming up to 242 DEG C with the technique from desulfurization reactor
Gas is mixed into methyl alcohol synthetic reactor.CO transformation and methanol synthesis reaction heat are moved back out by boiler water vapor, by-product 1500kg/h's
Saturated vapor (pressure 2.5MPa, temperature are 224 DEG C), sends to steam pipe network by drum.
The above embodiments and description only describe the principles of the invention, therefore do not limit this hair
Bright protection scope, under the premise of not departing from the inventive spirit of the present invention and range, this technology invention also have various change and
It improves, these changes and improvements all fall within the protetion scope of the claimed invention.Part that the present invention does not relate to is and the prior art
It is identical or can be realized by using the prior art.
Claims (8)
1. a kind of transformation methanolizing integrated production equipment, it is characterised in that: the device includes low-pressure steam generator (1), thick
Synthesize gas separating device (2), synthesis hot-air heater (3), detoxification slot (4), change furnace (5), desulfurization reactor (6), methyl alcohol synthetic reactor
(7), the crude synthesis gas pipeline from upstream coal gasification apparatus is connected with the input terminal of low-pressure steam generator (1), low-pressure steam
Generator (1) is connected by crude synthesis gas separator (2) with synthesis hot-air heater (3), and the synthesis hot-air heater (3) passes through
It is connected at the top of detoxification slot (4) and change furnace (5)；Change furnace (5) the bottom output end is by synthesis hot-air heater (3) and takes off
Reaction of Salmon-Saxl device (6) bottom is connected, and is connected at the top of output channel and methyl alcohol synthetic reactor (7) at the top of desulfurization reactor (6), methanol-fueled CLC
After tower (7) outlet at bottom rich methanol technique feed channel passes sequentially through circulating gas heater (8) and water cooler (9), into methanol point
From device (10), the bottom output liquid phase of methanol separator (10) is that crude carbinol product sends to out-of-bounds rectifier unit；Methanol separator
(10) top gas phase a part is sent to out-of-bounds as periodic off-gases, and another part successively passes through recycle gas compressor (11) and circulation
Hot-air heater (8) is connected with from desulfurization reactor (6) top exit technique feed channel afterwards, and methyl alcohol synthetic reactor is entered after mixing
(7)。
2. transformation methanolizing integrated production equipment according to claim 1, it is characterised in that: change furnace (5) and methanol
The vapor uptake of synthetic tower (7) is connected with drum (12) respectively, the boiler feedwater down-comer of drum (12) respectively with change furnace
(5) it is connected with methyl alcohol synthetic reactor (7).
3. transformation methanolizing integrated production equipment according to claim 1, it is characterised in that: during drum (12) is provided with
Press boiler feedwater supply pipeline and saturated vapor output out-of-bounds pipeline.
4. a kind of realize transformation methanolizing integrated production method using device described in claim 1, it is characterised in that: the party
Method the following steps are included:
(1) crude synthesis gas from coal gasification unit is entered after low-pressure steam generator (1) cooling and enters crude synthesis gas separation
Device (2) isolates high temperature condensate liquid and returns to gasification, and gas phase removes after entering synthesis hot-air heater (3) heating into detoxification slot (4)
Impurity carries out the hydrogen-carbon ratio that CO conversion reaction adjusts process gas into change furnace (5), obtains high temperature shift gas；
(2) high temperature shift gas enters synthesis hot-air heater (3), enters desulfurization reactor (6) after being cooled and removes H in process gas2S
Etc. harmful substances, then with the circulating air from recycle gas compressor be mixed into methyl alcohol synthetic reactor (7) generate methanol；
(3) after methyl alcohol synthetic reactor (7) exit gas enters first circulation hot-air heater (8) and second circulation hot-air heater (9), warp
Enter methanol separator (10) after crossing water cooler (9) cooling, liquid phase is that crude carbinol product goes rectification cell to refine, gas phase fixed gas
A part is used as periodic off-gases, and another part is after recycle gas compressor (11) pressurize, after circulating gas heater (8) heating
Methyl alcohol synthetic reactor (7) are mixed into the process gas from desulfurization reactor (6).
5. according to the method described in claim 4, it is characterized by: the crude synthesis gas of step (1) from upstream coal gasification unit
It is introduced into low-pressure steam generator by-product low-pressure saturated steam, to control the liquid to steam ratio of crude synthesis gas, after being cooled is in gas
The crude synthesis gas that liquid is two enters crude synthesis gas separator and carries out gas-liquid separation, and liquid phase is that high temperature condensate liquid returns to gasification, gas phase
Resulting process gas removes detoxification slot, and the liquid to steam ratio of crude synthesis gas controls between 0.1~0.6.
6. according to the method described in claim 4, it is characterized by: the process gas temperature into change furnace (5) is controlled 220
Between~280 DEG C, change furnace (5) is isothermal reactor, and operation temperature is controlled at 240~350 DEG C.
7. according to the method described in claim 4, it is characterized by: the process gas temperature into methyl alcohol synthetic reactor (7) controls
Between 200~250 DEG C, methyl alcohol synthetic reactor (7) is isothermal reactor, and operation temperature is controlled at 220~320 DEG C.
8. according to the method described in claim 4, it is characterized by: the first of the CO transformation and methyl alcohol synthetic reactor (7) of change furnace (5)
Alcohol synthesis reaction heat is moved back out by boiler water vapor, by-product saturated vapor, sends to steam pipe network by drum, and by-product saturation is steamed
The pressure of vapour is 2.0~4.5MPa.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109678659A (en) * | 2019-02-28 | 2019-04-26 | 中煤陕西榆林能源化工有限公司 | The parallel methanol synthesis reaction system of double-reactor |
| CN109772233A (en) * | 2019-02-28 | 2019-05-21 | 中煤陕西榆林能源化工有限公司 | Synthesis reaction system and methane synthesizing method with porous type central tube |
| CN110240948A (en) * | 2019-06-28 | 2019-09-17 | 中石化南京工程有限公司 | A kind of coal chemical industry temperature control transformation coproduction electrical energy system and method |
| CN111440049A (en) * | 2020-04-15 | 2020-07-24 | 陕西聚能新创煤化科技有限公司 | High-efficient methyl alcohol synthesis system |
| CN112142559A (en) * | 2020-09-22 | 2020-12-29 | 吕永华 | Waste heat recovery device for methanol production |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101429098A (en) * | 2008-12-03 | 2009-05-13 | 西南化工研究设计院 | Method for synthesis of methanol with CO, CO2 and H#[-2] |
| CN102531835A (en) * | 2010-04-20 | 2012-07-04 | 陕西延长石油（集团）有限责任公司 | Method for synthesizing methanol through low-carbon technology |
| CN104788285A (en) * | 2015-03-26 | 2015-07-22 | 七台河宝泰隆煤化工股份有限公司 | Methanol synthesis system |
| CN204917951U (en) * | 2015-07-20 | 2015-12-30 | 阳煤集团太原化工新材料有限公司 | Get rid of CO's in raw gas isothermal conversion systems |
| CN107074537A (en) * | 2014-11-06 | 2017-08-18 | 卡萨尔公司 | Method for producing synthesis gas |
| CN107164007A (en) * | 2017-05-15 | 2017-09-15 | 中石化南京工程有限公司 | A kind of method of non-stoichiometric isothermal synthetic natural gas |
| CN107162872A (en) * | 2017-04-28 | 2017-09-15 | 中石化宁波工程有限公司 | A kind of low pressure methanol synthesis technique |
-
2018
- 2018-10-25 CN CN201811250264.7A patent/CN109384647A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101429098A (en) * | 2008-12-03 | 2009-05-13 | 西南化工研究设计院 | Method for synthesis of methanol with CO, CO2 and H#[-2] |
| CN102531835A (en) * | 2010-04-20 | 2012-07-04 | 陕西延长石油（集团）有限责任公司 | Method for synthesizing methanol through low-carbon technology |
| CN107074537A (en) * | 2014-11-06 | 2017-08-18 | 卡萨尔公司 | Method for producing synthesis gas |
| CN104788285A (en) * | 2015-03-26 | 2015-07-22 | 七台河宝泰隆煤化工股份有限公司 | Methanol synthesis system |
| CN204917951U (en) * | 2015-07-20 | 2015-12-30 | 阳煤集团太原化工新材料有限公司 | Get rid of CO's in raw gas isothermal conversion systems |
| CN107162872A (en) * | 2017-04-28 | 2017-09-15 | 中石化宁波工程有限公司 | A kind of low pressure methanol synthesis technique |
| CN107164007A (en) * | 2017-05-15 | 2017-09-15 | 中石化南京工程有限公司 | A kind of method of non-stoichiometric isothermal synthetic natural gas |
Non-Patent Citations (3)
| Title |
|---|
| 王明华等: "煤制甲醇CO变换工艺组合方式的研究", 《化学工程》 * |
| 谭怀山: "大型煤制甲醇装置变换技术对比", 《大氮肥》 * |
| 黄琼: "甲醇合成的工艺过程分析与操作控制优化", 《中国优秀硕士学位论文全文数据库工程科技Ⅰ辑》 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109678659A (en) * | 2019-02-28 | 2019-04-26 | 中煤陕西榆林能源化工有限公司 | The parallel methanol synthesis reaction system of double-reactor |
| CN109772233A (en) * | 2019-02-28 | 2019-05-21 | 中煤陕西榆林能源化工有限公司 | Synthesis reaction system and methane synthesizing method with porous type central tube |
| CN110240948A (en) * | 2019-06-28 | 2019-09-17 | 中石化南京工程有限公司 | A kind of coal chemical industry temperature control transformation coproduction electrical energy system and method |
| CN111440049A (en) * | 2020-04-15 | 2020-07-24 | 陕西聚能新创煤化科技有限公司 | High-efficient methyl alcohol synthesis system |
| CN112142559A (en) * | 2020-09-22 | 2020-12-29 | 吕永华 | Waste heat recovery device for methanol production |
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