CN109399565A - A kind of system that SMR device reduces carbon distribution using steam preheating synthesis gas - Google Patents
A kind of system that SMR device reduces carbon distribution using steam preheating synthesis gas Download PDFInfo
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- CN109399565A CN109399565A CN201811635684.7A CN201811635684A CN109399565A CN 109399565 A CN109399565 A CN 109399565A CN 201811635684 A CN201811635684 A CN 201811635684A CN 109399565 A CN109399565 A CN 109399565A
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- China
- Prior art keywords
- synthesis gas
- high temperature
- pipeline
- temperature shift
- carbon distribution
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- Pending
Links
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 74
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 74
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 25
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 25
- 238000006243 chemical reaction Methods 0.000 claims abstract description 14
- 238000011084 recovery Methods 0.000 claims abstract description 14
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims abstract description 12
- 235000011941 Tilia x europaea Nutrition 0.000 claims abstract description 12
- 239000004571 lime Substances 0.000 claims abstract description 12
- 239000007789 gas Substances 0.000 claims description 59
- 230000001105 regulatory effect Effects 0.000 claims description 13
- 239000012495 reaction gas Substances 0.000 claims description 9
- 238000010992 reflux Methods 0.000 claims description 9
- 230000008676 import Effects 0.000 claims description 4
- 239000007788 liquid Substances 0.000 claims 1
- 238000002156 mixing Methods 0.000 abstract description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 5
- 239000001257 hydrogen Substances 0.000 description 5
- 238000000034 method Methods 0.000 description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- 230000008569 process Effects 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000012544 monitoring process Methods 0.000 description 2
- 238000010792 warming Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000000629 steam reforming Methods 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/48—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents followed by reaction of water vapour with carbon monoxide
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
The present invention relates to the systems that a kind of SMR device reduces carbon distribution using steam preheating synthesis gas, including high temperature shift reactor, synthesize air preheater, low-pressure steam pipeline, high pressure steam line, synthesis gas pipeline, lime set recovery line, the synthesis air preheater contains two heat exchanger channels, the entrance of first heat exchanger channels is connected with low-pressure steam pipeline, the outlet of first heat exchanger channels is connected with lime set recovery line, the entrance of Article 2 heat exchanger channels is connected with synthesis gas pipeline, the outlet of Article 2 heat exchanger channels is connected with synthesis gas preheating rear line, the synthesis gas preheating rear line and high pressure steam line enter high temperature shift reactor after crossing.Compared with prior art, the present invention enters high temperature shift reactor after still further introducing high steam mixing to synthesis gas pipeline, inhibits the generation of carbon distribution reaction using low-pressure steam first by synthesis gas steam preheating to 100~200 DEG C.
Description
Technical field
The present invention relates to SMR devices, are using what steam preheating synthesis gas reduced carbon distribution more particularly, to a kind of SMR device
System.
Background technique
SMR device is the device using natural gas and steam reforming reaction hydrogen manufacturing, and reaction equation is as follows:
CnHm+n H2O→n CO+(n+m/2)H2
CO+H2O→CO2+H2
At 550~650 DEG C, outlet temperature is controlled at 800~900 DEG C the control of reburner inlet temperature.
Under this high temperature, the hydrocarbon in most of charging is changed into CO, for device for producing hydrogen, needs to pass through CO
High temperature shift hydrogen making.Reaction equation is as follows:
CO+H2O→CO2+H2
At 300~350 DEG C, outlet temperature is controlled at 400~500 DEG C the control of high temperature shift reactor inlet temperature.
It, can be in high temperature shift reactor import increase synthesis gas all the way for more hydrogen makings in HYCO factory
Admission line utilizes the more hydrogen makings of high temperature shift reactor.Synthesis gas enters high temperature shift reactor and is preheated, and leads to
It is often to be preheated using SMR waste heat recovery stage, synthesis gas heater outlet temperature is controlled at 250~300 DEG C.And the mistake preheated
Carbon distribution reaction often occurs for journey, and reaction equation is as follows:
2CO→C+CO2
Carbon dust can adhere on high temperature shift reactor catalyst, and influence catalyst activity.
Summary of the invention
It is an object of the present invention to overcome the above-mentioned drawbacks of the prior art and provide a kind of SMR devices to utilize steaming
The system of vapour pre-heated synthesis gas reduction carbon distribution.
The present invention utilizes low-pressure steam first by synthesis gas steam preheating to 100~200 DEG C, still further to synthesis gas pipeline
Enter high temperature shift reactor after introducing high steam mixing, inhibits the generation of carbon distribution reaction.
The purpose of the present invention can be achieved through the following technical solutions:
A kind of system that SMR device reduces carbon distribution using steam preheating synthesis gas, including high temperature shift reactor, synthesis gas
Preheater, low-pressure steam pipeline, high pressure steam line, synthesis gas pipeline, lime set recovery line,
The synthesis air preheater contains two heat exchanger channels, entrance and the low-pressure steam pipeline phase of first heat exchanger channels
Even, the outlet of first heat exchanger channels is connected with lime set recovery line, entrance and the synthesis gas pipeline phase of Article 2 heat exchanger channels
Even, the outlet of Article 2 heat exchanger channels is connected with synthesis gas preheating rear line, the synthesis gas preheating rear line and high steam
Pipeline enters high temperature shift reactor after crossing.
The high temperature shift reactor includes the entrance of upper end and the outlet of lower end, and the synthesis gas preheats rear line and height
Pressure steam pipe line enters the entrance of high temperature shift reactor after crossing.
The outlet of the high temperature shift reactor is connected with gas pipeline is reacted, and the reaction gas pipeline is used for high temperature shift
Product exports after reaction.
The import of the high temperature shift reactor is also connected with reaction gas reflux pipeline, and the reaction gas reflux pipeline is used for
By product reflux after part high temperature shift reaction to high temperature shift reactor.
The low-pressure steam pipeline is equipped with hand valve, regulating valve and flowmeter.
The high pressure steam line is equipped with hand valve, regulating valve and flowmeter.
The synthesis gas pipeline is equipped with regulating valve and flowmeter.
The lime set recovery line is equipped with hand valve.
The synthesis gas preheating rear line is equipped with thermocouple.
The high temperature shift reactor inlet is equipped with thermocouple.
Synthesis air preheater is carried out first to be preheated to predetermined temperature, synthesis air preheater preheating by low-pressure steam pipeline
To 100~200 DEG C.High pressure steam line carries out being preheated to predetermined temperature, that is, uses temperature.
The regulating valve on synthesis gas pipeline, synthesis gas pipeline and low-pressure steam pipeline is opened to carry out by synthesis air preheater
Heat exchange is discharged by lime set recovery line after low-pressure steam cooling, after synthesis gas is warming up to preheating temperature, is preheated by synthesis gas
Rear line enters high temperature shift reactor after crossing with high pressure steam line and is reacted.
In the above process, the opening and closing that pipeline is realized by hand valve is realized the adjusting of uninterrupted by regulating valve, passed through
Flowmeter monitors uninterrupted, passes through thermocouple monitoring temperature.
The present invention utilizes low-pressure steam first by synthesis gas steam preheating to 100~200 DEG C, still further to synthesis gas pipeline
Enter high temperature shift reactor after introducing high steam mixing, inhibits the generation of carbon distribution reaction.
Compared with prior art, the invention has the following advantages that
1, synthesis gas is first preheated, but not up to or process carbon distribution reaction temperature.
2, after synthesis gas is mixed with a certain proportion of high steam, reach reaction temperature and inhibit the generation of carbon distribution reaction.
Detailed description of the invention
Fig. 1 is the system structure diagram that SMR device reduces carbon distribution using steam preheating synthesis gas.
Specific embodiment
The present invention is described in detail with specific embodiment below in conjunction with the accompanying drawings.
Embodiment
A kind of system that SMR device reduces carbon distribution using steam preheating synthesis gas, as shown in Figure 1, including that high temperature shift is anti-
Answer device R01, synthesis air preheater E01, low-pressure steam pipeline 11, high pressure steam line 12, synthesis gas pipeline 13, lime set recovery tube
Line 14, synthesis air preheater E01 contain two heat exchanger channels, entrance and 11 phase of low-pressure steam pipeline of first heat exchanger channels
Even, the outlet of first heat exchanger channels is connected with lime set recovery line 14, the entrance and synthesis gas pipeline of Article 2 heat exchanger channels
13 are connected, and the outlet of Article 2 heat exchanger channels is connected with synthesis gas preheating rear line 15, and synthesis gas preheats rear line 15 and high pressure
Steam pipe line 12 enters high temperature shift reactor R01 after crossing.
High temperature shift reactor R01 includes the entrance of upper end and the outlet of lower end, and synthesis gas preheats rear line 15 and high pressure
Steam pipe line 12 enters the entrance of high temperature shift reactor R01 after crossing.The outlet of high temperature shift reactor R01 with react tracheae
Line 16 is connected, and reaction gas pipeline 16 is exported for product after reacting high temperature shift.The import of high temperature shift reactor R01 also with
Reaction gas reflux pipeline 17 is connected, and reaction gas reflux pipeline 17 is used to become product reflux to high temperature after part high temperature shift reaction
Change reactor R01.
Low-pressure steam pipeline 11 is equipped with hand valve 1, regulating valve 2 and flowmeter 3.High pressure steam line 12 be equipped with hand valve 1,
Regulating valve 2 and flowmeter 3.Synthesis gas pipeline 13 is equipped with regulating valve 2 and flowmeter 3.Lime set recovery line 14 is equipped with hand valve
1.Synthesis gas preheats rear line 15 and is equipped with thermocouple 4.The inlet high temperature shift reactor R01 is equipped with thermocouple 4.
Synthesis air preheater E01 is carried out first to be preheated to predetermined temperature, synthesis gas preheating by low-pressure steam pipeline 11
Device E01 is preheated to 100~200 DEG C.High pressure steam line 12 carries out being preheated to predetermined temperature, that is, uses temperature.
The regulating valve on synthesis gas pipeline 13, synthesis gas pipeline 13 and low-pressure steam pipeline 11 is opened to preheat by synthesis gas
Device E01 exchanges heat, and is discharged after low-pressure steam cooling by lime set recovery line 14, after synthesis gas is warming up to preheating temperature, leads to
It crosses after synthesis gas preheating rear line 15 crosses with high pressure steam line 12 and is reacted into high temperature shift reactor R01.
In the above process, the opening and closing that pipeline is realized by hand valve is realized the adjusting of uninterrupted by regulating valve, passed through
Flowmeter monitors uninterrupted, passes through thermocouple monitoring temperature.
The above description of the embodiments is intended to facilitate ordinary skill in the art to understand and use the invention.
Person skilled in the art obviously easily can make various modifications to these embodiments, and described herein general
Principle is applied in other embodiments without having to go through creative labor.Therefore, the present invention is not limited to the above embodiments, ability
Field technique personnel announcement according to the present invention, improvement and modification made without departing from the scope of the present invention all should be of the invention
Within protection scope.
Claims (10)
1. the system that a kind of SMR device reduces carbon distribution using steam preheating synthesis gas, which is characterized in that reacted including high temperature shift
Device (R01), low-pressure steam pipeline (11), high pressure steam line (12), synthesis gas pipeline (13), coagulates at synthesis air preheater (E01)
Liquid recovery line (14),
The synthesis air preheater (E01) contains two heat exchanger channels, the entrance and low-pressure steam pipeline of first heat exchanger channels
(11) it is connected, the outlet of first heat exchanger channels is connected with lime set recovery line (14), the entrance of Article 2 heat exchanger channels and conjunction
It is connected at gas pipeline (13), the outlet of Article 2 heat exchanger channels is connected with synthesis gas preheating rear line (15), and the synthesis gas is pre-
Hot rear line (15) and high pressure steam line (12) enter high temperature shift reactor (R01) after crossing.
2. the system that a kind of SMR device according to claim 1 reduces carbon distribution using steam preheating synthesis gas, feature exist
In the high temperature shift reactor (R01) includes the entrance of upper end and the outlet of lower end, and the synthesis gas preheats rear line (15)
Enter the entrance of high temperature shift reactor (R01) after crossing with high pressure steam line (12).
3. the system that a kind of SMR device according to claim 2 reduces carbon distribution using steam preheating synthesis gas, feature exist
In the outlet of the high temperature shift reactor (R01) is connected with gas pipeline (16) are reacted, and the reaction gas pipeline (16) is used for will
Product exports after high temperature shift reaction.
4. the system that a kind of SMR device according to claim 3 reduces carbon distribution using steam preheating synthesis gas, feature exist
In the import of the high temperature shift reactor (R01) is also connected with reaction gas reflux pipeline (17), the reaction gas reflux pipeline
(17) for product reflux after reacting part high temperature shift to high temperature shift reactor (R01).
5. the system that a kind of SMR device according to claim 1 reduces carbon distribution using steam preheating synthesis gas, feature exist
Hand valve (1), regulating valve (2) and flowmeter (3) are equipped in, the low-pressure steam pipeline (11).
6. the system that a kind of SMR device according to claim 1 reduces carbon distribution using steam preheating synthesis gas, feature exist
Hand valve (1), regulating valve (2) and flowmeter (3) are equipped in, the high pressure steam line (12).
7. the system that a kind of SMR device according to claim 1 reduces carbon distribution using steam preheating synthesis gas, feature exist
In the synthesis gas pipeline (13) is equipped with regulating valve (2) and flowmeter (3).
8. the system that a kind of SMR device according to claim 1 reduces carbon distribution using steam preheating synthesis gas, feature exist
In the lime set recovery line (14) is equipped with hand valve (1).
9. the system that a kind of SMR device according to claim 1 reduces carbon distribution using steam preheating synthesis gas, feature exist
In synthesis gas preheating rear line (15) is equipped with thermocouple (4).
10. the system that a kind of SMR device according to claim 2 reduces carbon distribution using steam preheating synthesis gas, feature
It is, the high temperature shift reactor inlet (R01) is equipped with thermocouple (4).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811635684.7A CN109399565A (en) | 2018-12-29 | 2018-12-29 | A kind of system that SMR device reduces carbon distribution using steam preheating synthesis gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811635684.7A CN109399565A (en) | 2018-12-29 | 2018-12-29 | A kind of system that SMR device reduces carbon distribution using steam preheating synthesis gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN109399565A true CN109399565A (en) | 2019-03-01 |
Family
ID=65462141
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201811635684.7A Pending CN109399565A (en) | 2018-12-29 | 2018-12-29 | A kind of system that SMR device reduces carbon distribution using steam preheating synthesis gas |
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101062763A (en) * | 2006-04-25 | 2007-10-31 | 王庆松 | Hydrogen production technique |
| US20120148485A1 (en) * | 2010-12-09 | 2012-06-14 | Morrow Jeffrey M | Steam methane reforming process |
| CN103982165A (en) * | 2014-05-21 | 2014-08-13 | 中国石油大学(北京) | Method for extracting natural gas hydrate by using gas mixture of CO2 and H2 |
| CN107416769A (en) * | 2017-08-03 | 2017-12-01 | 山西潞安煤基合成油有限公司 | A kind of method that methane carbon dioxide reformation prepares synthesis gas |
| CN107746039A (en) * | 2017-12-05 | 2018-03-02 | 聂国印 | A kind of method and apparatus of methane and carbon dioxide without catalytic reforming preparing synthetic gas |
| CN208135895U (en) * | 2018-03-22 | 2018-11-23 | 上海华林工业气体有限公司 | Steam reformer flue gas heat recycling system |
| CN209567806U (en) * | 2018-12-29 | 2019-11-01 | 上海华林工业气体有限公司 | The system that SMR device reduces carbon distribution using steam preheating synthesis gas |
-
2018
- 2018-12-29 CN CN201811635684.7A patent/CN109399565A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101062763A (en) * | 2006-04-25 | 2007-10-31 | 王庆松 | Hydrogen production technique |
| US20120148485A1 (en) * | 2010-12-09 | 2012-06-14 | Morrow Jeffrey M | Steam methane reforming process |
| CN103982165A (en) * | 2014-05-21 | 2014-08-13 | 中国石油大学(北京) | Method for extracting natural gas hydrate by using gas mixture of CO2 and H2 |
| CN107416769A (en) * | 2017-08-03 | 2017-12-01 | 山西潞安煤基合成油有限公司 | A kind of method that methane carbon dioxide reformation prepares synthesis gas |
| CN107746039A (en) * | 2017-12-05 | 2018-03-02 | 聂国印 | A kind of method and apparatus of methane and carbon dioxide without catalytic reforming preparing synthetic gas |
| CN208135895U (en) * | 2018-03-22 | 2018-11-23 | 上海华林工业气体有限公司 | Steam reformer flue gas heat recycling system |
| CN209567806U (en) * | 2018-12-29 | 2019-11-01 | 上海华林工业气体有限公司 | The system that SMR device reduces carbon distribution using steam preheating synthesis gas |
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Effective date of abandoning: 20240621 |