CN206266222U - A kind of coal hydrogen manufacturing CO converts multi-joint-production apparatus - Google Patents
A kind of coal hydrogen manufacturing CO converts multi-joint-production apparatus Download PDFInfo
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- CN206266222U CN206266222U CN201620312482.9U CN201620312482U CN206266222U CN 206266222 U CN206266222 U CN 206266222U CN 201620312482 U CN201620312482 U CN 201620312482U CN 206266222 U CN206266222 U CN 206266222U
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- 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
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- 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
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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Abstract
The utility model is related to a kind of coal hydrogen manufacturing CO conversion multi-joint-production apparatus, including the first reacting furnace（3）, the second reacting furnace（5）With the 3rd reacting furnace（6）；The output channel of crude synthesis gas and the first gas-liquid separator（1）It is connected, first gas-liquid separator（1）Gaseous phase outlet pass through crude synthesis gas heater（2）With the first reacting furnace（3）Input be connected, first reacting furnace（3）Output end pass sequentially through crude synthesis gas heater（2）, the first waste heat boiler（4）With the second reacting furnace（5）Input be connected.According to supply system theoretical principles such as " temperature counterpart, cascade utilizations ", the utility model introduces the design concept of cool and thermal power Poly-generation, by series circulation working medium generating set, absorption refrigeration unit and heating heater in carbon monoxide transformation technical, while meeting production technology and ensureing CO conversion requirements, effective recycling conversion process reaction heat, the Poly-generation that generates electricity, freezes and heat can be realized, energy-saving notable, utilization rate of waste heat is high.
Description
Technical field
The utility model belongs to the optimization of coal chemical engineering equipment energy saving technology and factory's technical field of waste heat recycling, is related to one
Coal hydrogen manufacturing CO conversion multi-joint-production apparatus are planted, is the industrial applications in chemical production device of distributed energy resource system.
Background technology
Industrially, energy-conserving and environment-protective industry, optimize technique technology path, reasonable disposition resource, popularization and application are accelerated development
Power-saving technology, using energy-efficient equipment, promote industrial upgrading and development pattern transformation, tool is of great significance.It is cold and hot
Electric Poly-generation is one kind of distributed energy, with energy saving, improves environment, increases the comprehensive benefits such as supply of electric power, is city
One of necessary means of city's control atmosphere pollution and raising comprehensive utilization of energy rate, meet National Sustainable Development Strategies.《China
People's republic's economizing energy law》39th article is pointed out that " country encourages development heat-cascading technology, thermoelectric cold cogeneration skill
Art, improves heat integration rate ".Country's hair in 2006 changes the departments such as the same Ministry of Finance of meeting, the Ministry of Construction and works out《Eleventh Five-Year Plan ten
Big emphasis energy conservation project implementation guideline》, clearly propose " building distributed combined heat and power generation and heat-electricity-cold combined supply ".
In coal hydrogen manufacturing production, the content usually from CO in the crude synthesis gas of upstream coal gasification apparatus is more, or even high
Up to more than 70%, it is therefore desirable to CO and water reaction are changed into CO by becoming switching catalytic reaction2And H2, obtain the work rich in hydrogen
Skill gas, then by downstream acid gas removal unit removing CO2Deng impurity, the hydrogen of high-purity is obtained.Carbon monodixe conversion is anti-
Strong exothermal reaction should be belonged to, be a process for balance controlled, the hot(test)-spot temperature of reaction is up to more than 450 DEG C.At present, industry
Most of CO shift reaction is connected using mutil-stage adiabatic reactor in production, so as to reach carbon monoxide in process gas
High-conversion rate.However, a large amount of reaction recuperations of heat of CO conversion processes are by setting many heat exchangers, by-product low pressure steam,
Preboiler feeds water, heats the modes such as desalted water and circulating water to realize.
In in September, 2011《Middle nitrogenous fertilizer》In disclose entitled " Shell coal gasifications WGR CO sulfur resistant conversion process high
The article of process optimization ", is given up in the shift process discussed in text by pressure in series connection useless pot, middle pressure steam superheater and low pressure
Pot, the mode that vapours and low-pressure steam are pressed through in by-product reclaims reaction heat, and proposes Optimized Measures.Disclosed special
In sharp file, such as " a kind of saturated hot-water tower height WGR CO conversion process (CN102337159A) ", " one kind is powdered coal pressuring gasified
The CO raw gas conversion process high for obtaining " (CN104340958A) and a kind of " share split circulation CO conversion process
(CN103881765A), carbon monoxide transformation process reaction heat is all the superheated steam and saturated vapor for each grade of by-product,
Most of steam grades of usual by-product are low, capacity usage ratio is low, and the great quantities of spare steam often directly emptying discharge of generation is made
Into the significant wastage of the energy.
Above-described conversion process flow arrangement using multistage reactor series connection waste heat boiler, is returned by byproduct steam
Reaction heat is received, that is, give up pot shift process, although disclosure satisfy that the requirement in technique productions, it is disadvantageous in that：Device is transported
Row high energy consumption, heating efficiency is low, and byproduct steam amount is big, and steam grade is low, there is great quantities of spare steam evacuation in actual production,
High efficiente callback course of reaction heat is unable to, energy waste is caused.
Utility model content
The purpose of this utility model is according to the development of national energy-saving emission reduction and relevant policies requirement, for prior art
The weak point of presence, and a kind of coal hydrogen manufacturing CO conversion multi-production process and device are provided.According to " temperature counterpart, cascade utilization "
Deng supply system theoretical principle, optimize and build technological process, propose first in Coal Chemical Industry production technology device, by introducing
Cool and thermal power Poly-generation is used to recycle reaction heat, while meeting technique productions requirement, realizes generating electricity, freeze and heating
Multiple-supplying, and with energy integrated result it is good, it is energy-saving significantly, utilization rate of waste heat is high the features such as.
The purpose of this utility model can be achieved through the following technical solutions：
A kind of coal hydrogen manufacturing CO converts multi-joint-production apparatus, and the device includes the first reacting furnace, the second reacting furnace and the 3rd reaction
Stove；
The output channel of crude synthesis gas is connected with the first gas-liquid separator, and the gas phase of first gas-liquid separator (1) goes out
Mouth is connected by crude synthesis gas heater (2) with the input of the first reacting furnace (3), the output end of first reacting furnace (3)
Crude synthesis gas heater (2), the first waste heat boiler (4) is passed sequentially through to be connected with the input of the second reacting furnace (5)；
The output end of second reacting furnace is connected by the second waste heat boiler with the input of the 3rd reacting furnace, and described
The output end of three reacting furnaces is connected with the second gas-liquid separator, and the output end at the top of second gas-liquid separator passes through generator
It is connected with the 3rd gas-liquid separator, the output end at the top of the 3rd gas-liquid separator is by heating heater and the 4th gas-liquid point
It is connected from device, the output end at the top of the 4th gas-liquid separator is connected by conversion gas end cooler with the 5th gas-liquid separator,
Output end at the top of 5th gas-liquid separator is connected with depickling unit.
In technical solutions of the utility model：The first described waste heat boiler matches phase with first circulation working medium generating set
Even；The second described waste heat boiler is connected with the matching of second circulation working medium generating set；Described generator and absorption refrigeration
EGR matching is connected.
In technical solutions of the utility model：Described first circulation working medium generating set, second circulation working medium generating set
It is the circulation of card Linne, Rankine cycle or their modified version；Described absorption type refrigerating unit be thermal drivers kind of refrigeration cycle or
Heat/work(composite flooding kind of refrigeration cycle.The cycle fluid that described absorption type refrigerating unit is used for lithium bromide-water, ammoniacal liquor,
R134a-DMF or ionic liquid-water.
In some preferred technical schemes：The output end of first reacting furnace pass sequentially through crude synthesis gas heater,
The input of the first waste heat boiler and the second reacting furnace is connected.
In some preferred technical schemes：The output end of the 3rd reacting furnace passes through the second waste heat boiler and the second gas
Liquid/gas separator is connected.
A kind of utilization said apparatus realize the method that coal hydrogen manufacturing CO converts Poly-generation, and the method is comprised the following steps：
1) it is laggard by crude synthesis gas heater heat temperature raising after crude synthesis gas enter the first gas-liquid separator gas-liquid separation
Entering the first reacting furnace carries out adiabatic transformationreation, and the high temperature shift gas of gained enters the first waste heat boiler through crude synthesis gas heater
Drive and generate electricity；
2) step 1) drive the conversion gas lowered the temperature after generating electricity to be reacted into the second reacting furnace, reacted gas conveying
The second waste heat boiler to second circulation working medium generating set drives generating；
3) step 2) drive the conversion gas lowered the temperature after generating electricity to be reacted into the 3rd reacting furnace, reacted gas is again
The second waste heat boiler for being delivered to second circulation working medium generating set drives generating；
4) step 3) drive the cooling that generates electricity after gas be introduced into the second gas-liquid separator, it is separated after the gas phase that obtains go to inhale
The generator of receipts formula refrigerating plant, from generator conversion gas out enter the 3rd gas-liquid separator, be separated after the gas that obtains
Body is delivered to heating heater, the gas after cooling is delivered to the 4th gas-liquid separator, from the 4th gas-liquid separation device out
Gas is delivered to conversion gas end cooler and the 5th gas-liquid separator successively, and downstream is delivered to from the 5th gas-liquid separator gas out
Sour gas deviates from unit.
In the above-mentioned method for realizing coal hydrogen manufacturing CO conversion Poly-generation：First reacting furnace, the second reacting furnace, the 3rd reacting furnace
Inlet temperature is controlled between 200~300 DEG C, and at 350~500 DEG C, the second reacting furnace goes out for the first reaction heater outlet temperature control
, at 250~400 DEG C, the 3rd reaction heater outlet temperature control is at 200~300 DEG C for mouth temperature control.
In the above-mentioned method for realizing coal hydrogen manufacturing CO conversion Poly-generation：First waste heat of the first circulation working medium generating set
The operation temperature of boiler is 300~500 DEG C；The operation temperature of the second waste heat boiler of second circulation working medium generating set is 200
~300 DEG C；The operation temperature of absorption type refrigerating unit generator is 100~200 DEG C；The hot water temperature that heating heater can be provided
Spend is 50~100 DEG C.
In the above-mentioned method for realizing coal hydrogen manufacturing CO conversion Poly-generation：Crude synthesis gas derive from coal water slurry gasifying device, fine coal
Gasification installation or fluidized gasification device.
In technical solutions of the utility model：CO reaction heats are used to generate electricity, are freezed and heating；Wherein, the first reaction
The pyroreaction thermal drivers first circulation working medium TRT of stove realizes that electric energy is exported；The pyroreaction of second, third reacting furnace
Hot common driving second circulation working medium TRT realizes that electric energy is exported；3rd reacting furnace conversion gas out first pass through second and follow
Go to drive absorption type refrigerating unit to realize that cold is exported after ring working medium TRT and gas-liquid separator, then by gas-liquid separator
Heating heater heating water is removed after separating condensate liquid, heating hot water is provided the user.
In technical solutions of the utility model：The second waste heat boiler that the second circulation working medium generating set is used is double heat
Source unitized exchanger.
In technical solutions of the utility model：First reacting furnace, the second reacting furnace and the 3rd reacting furnace are axial-radial flow reactor,
Using insulation fix bed structure.
The beneficial effects of the utility model：
According to the development of national energy-saving emission reduction and relevant policies requirement, it is according to the total energy such as " temperature counterpart, cascade utilization "
System theoretical principle, optimizes and builds the Coal Chemical Industry technological process of production, introduces cool and thermal power Poly-generation mentality of designing, proposes in an oxidation
Two sets of cycle fluid generating sets, a set of absorption refrigeration unit and heating heaters of series connection in carbon conversion process, effectively reclaim
Using CO reaction heats, the Poly-generation that generates electricity, freezes and heat can be simultaneously realized, and with energy integrated result is good, energy-conservation
The features such as consumption reduction is significantly, utilization rate of waste heat is high.
Brief description of the drawings
Fig. 1 is process flow diagram of the present utility model.
In figure：The gas-liquid separators of 1- first, 2- crude synthesis gas heaters, the reacting furnaces of 3- first, the waste heat boilers of 4- first, 5-
Second reacting furnace, the reacting furnaces of 6- the 3rd, the waste heat boilers of 7- second, the gas-liquid separators of 8- second, 9- generators, the gas-liquids of 10- the 3rd
Separator, 11- heating heaters, the gas-liquid separators of 12- the 4th, 13- conversion gas end cooler, the gas-liquid separators of 14- the 5th, 15-
First circulation working medium generating set, 16- second circulation working medium generating sets, 17- absorption type refrigeration circulation devices.
Specific embodiment
The utility model is described further with reference to embodiment, but protection domain of the present utility model is not limited to
This：
A kind of coal hydrogen manufacturing CO converts multi-joint-production apparatus, and the device includes the first reacting furnace (3), the second reacting furnace (5) and the
Three reacting furnaces (6)；
The output channel of crude synthesis gas is connected with the first gas-liquid separator (1), the output of first gas-liquid separator (1)
End is connected by crude synthesis gas heater (2) with the input of the first reacting furnace (3), the output end of first reacting furnace (3)
Crude synthesis gas heater (2), the first waste heat boiler (4) is passed sequentially through to be connected with the input of the second reacting furnace (5).
The output end of second reacting furnace (5) passes through the input phase of the second waste heat boiler (7) and the 3rd reacting furnace (6)
Even, the output end of the 3rd reacting furnace (6) is connected by the second waste heat boiler (7) with the second gas-liquid separator (8), and described the
Output end at the top of two gas-liquid separators (8) is connected by generator (9) with the 3rd gas-liquid separator (10), the 3rd gas-liquid
Output end at the top of separator (10) is connected by heating heater (11) with the 4th gas-liquid separator (12), the 4th gas-liquid
Output end at the top of separator (12) is connected by conversion gas end cooler (13) with the 5th gas-liquid separator (14), the 5th gas
Output end at the top of liquid/gas separator (14) is connected with depickling unit.
Described the first waste heat boiler (4) is connected with first circulation working medium generating set (15) matching；Described more than second
Heat boiler (7) is connected with second circulation working medium generating set (16) matching；Described generator (9) is filled with Absorption Cooling System
(17) matching is put to be connected.
First, second described cycle fluid generating set is card Linne circulation (Kalina Cycle), Rankine cycle
(Rankine Cycle) and their modified version；Described absorption type refrigerating unit is thermal drivers kind of refrigeration cycle and heat/work(
Composite flooding kind of refrigeration cycle and its modified version.
The cycle fluid that described absorption type refrigerating unit is used is lithium bromide-water, ammoniacal liquor, R134a-DMF, ionic liquid
Body-water and its modified version.
Example 1：Application in coal water slurry gasification device for producing hydrogen
318340Nm from upstream water-coal-slurry coal gasification apparatus3/ h crude synthesis gas (216 DEG C, 3.89MPa, WGR is
1.4), wherein CO contents be 44% (butt, v), into after the first gas-liquid separator (1) gas-liquid separation, by crude synthesis gas plus
After hot device (2) carries out adiabatic transformationreation after being warming up to 280 DEG C into the first reacting furnace (3), 439 DEG C of high temperature shift gas is obtained
After crude synthesis gas heater (2) is cooled to 377 DEG C, into the first waste heat boiler of first circulation working medium generating set (15)
(4) drive and generate electricity, the operation temperature of the first waste heat boiler cycle fluid outlet is 350 DEG C；Conversion gas are cooled to the change after 235 DEG C
Ventilation enters the second reacting furnace (5) and is reacted, and outlet conversion gas temperature is 254 DEG C, into second circulation working medium generating set
(16) the second waste heat boiler (7)；The conversion gas after 220 DEG C are cooled to be reacted into the 3rd reacting furnace (6), it is reacted
Conversion gas temperature is 221 DEG C, into second waste heat boiler (7) of second circulation working medium generating set (16), the second waste heat boiler
The operation temperature of cycle fluid outlet is 200 DEG C；Conversion gas enter the second gas-liquid separator (8) after being cooled to 168 DEG C, and gas phase is gone
The generator (9) of absorption type refrigerating unit (17) drives refrigeration, liquid phase to send out out-of-bounds；From absorption type refrigerating unit (17) out
After conversion gas separate lime set after being cooled to 110 DEG C through the 3rd gas-liquid separator (10), into heating heater (11), conversion gas quilt
After being cooled to 60 DEG C, by the 4th gas-liquid separator (12), sent after conversion gas end cooler (13) and the 5th gas-liquid separator (14)
Remove downstream sour gas abjection unit.110 DEG C of gained, 96.4t/h high temperature condensate liquid returns to upstream device reuse, and 7.03t/h is low
Warm condensate liquid sends to downstream sour water stripping (SWS) device.
The cold and hot electric output of CO converting means of table 1
Example 2：Application in coal gasification device for producing hydrogen
529121Nm from upstream gasifying powder coal device3(206 DEG C, 3.94MPa WGRs are for 0.92) for/h crude synthesis gas
Wherein CO contents are 69.8% (butt, v), into after the first gas-liquid separator (1) gas-liquid separation, by crude synthesis gas heater
(2) after carrying out adiabatic transformationreation into the first reacting furnace (3) after being warming up to 210 DEG C, the high temperature shift gas for obtaining 486 DEG C passes through
After crude synthesis gas heater (2) is cooled to 482 DEG C, into first waste heat boiler (4) of first circulation working medium generating set (15)
Drive and generate electricity, the operation temperature of the first waste heat boiler cycle fluid outlet is 350 DEG C；Conversion gas are cooled to the conversion after 215 DEG C
Gas is reacted into the second reacting furnace (5), and outlet conversion gas temperature is 289 DEG C, into second circulation working medium generating set
(16) the second waste heat boiler (7)；The conversion gas after 220 DEG C are cooled to be reacted into the 3rd reacting furnace (6), it is reacted
Conversion gas temperature is 234 DEG C, into second waste heat boiler (7) of second circulation working medium generating set (16), the second waste heat boiler
The operation temperature of cycle fluid outlet is 200 DEG C；Conversion gas enter the second gas-liquid separator (8) after being cooled to 168 DEG C, and gas phase is gone
The generator (9) of absorption type refrigerating unit (17) drives refrigeration, liquid phase to send out out-of-bounds；From absorption type refrigerating unit (17) out
After conversion gas separate lime set after being cooled to 106 DEG C through the 3rd gas-liquid separator (10), into heating heater (11), conversion gas quilt
After being cooled to 60 DEG C, by the 4th gas-liquid separator (12), sent after conversion gas end cooler (13) and the 5th gas-liquid separator (14)
Remove downstream sour gas abjection unit.106 DEG C of gained, 40.26t/h high temperature condensate liquid returns to upstream device reuse, 14.64t/h
Low temperature cold lime set sends to downstream sour water stripping (SWS) device.
The cold and hot electric output of CO converting means of table 2
Example 3：Application in fluidized bed coal gasification device for producing hydrogen
444254Nm from upstream fluidized bed coal gasification device3/ h crude synthesis gas (177 DEG C, 2.85Mpa, WGR is
0.48), wherein CO contents are 38.3% (butt, v), into after the first gas-liquid separator (1) gas-liquid separation, by crude synthesis gas
After heater (2) carries out adiabatic transformationreation after being warming up to 220 DEG C into the first reacting furnace (3), 404 DEG C of high temperature shift is obtained
Gas after crude synthesis gas heater (2) is cooled to 364 DEG C, into first circulation working medium generating set (15) the first waste heat pot
Stove (4) drives and generates electricity, and the operation temperature of the first waste heat boiler cycle fluid outlet is 350 DEG C；After conversion gas are cooled to 230 DEG C
Conversion gas are reacted into the second reacting furnace (5), and outlet conversion gas temperature is 279 DEG C, into second circulation working medium generator
Second waste heat boiler (7) of group (16)；It is cooled to the conversion gas after 220 DEG C to be reacted into the 3rd reacting furnace (6), after reaction
Conversion gas temperature be 234 DEG C, into second waste heat boiler (7) of second circulation working medium generating set (16), the second waste heat pot
The operation temperature of stove cycle fluid outlet is 200 DEG C；Conversion gas enter the second gas-liquid separator (8), gas phase after being cooled to 168 DEG C
The generator (9) of absorption type refrigerating unit (17) is gone to drive refrigeration, liquid phase to send out out-of-bounds；From absorption type refrigerating unit (17) out
Conversion gas be cooled to 110 DEG C after through the 3rd gas-liquid separator (10) separate lime set after, into heating heater (11), conversion gas
After being cooled to 60 DEG C, by the 4th gas-liquid separator (12), after conversion gas end cooler (13) and the 5th gas-liquid separator (14)
Send to downstream sour gas abjection unit.110 DEG C of gained, 14.45t/h high temperature condensate liquid returns to upstream device reuse, 15.27t/
H low temperature cold lime sets send to downstream sour water stripping (SWS) device.
The CO converting means cool and thermal powers Poly-generation of table 3 is exported
The output quantity of different hydrogen production from coal gasification mode cool and thermal powers in three examples is compared, as shown in table 4.Can be with root
According to user to the different demands of cold and hot electric output, corresponding coal gasifying process is selected, as the crude synthesis gas of CO conversion process
Source.
The different hydrogen production from coal gasification Poly-generation outputs of 4 three kinds of table are compared (based on 1000Nm3/ h crude synthesis gas)
| Form of energy | Coal water slurry gasification | Coal gasification | Fluidized bed coal gasification |
| Generated energy (kW) | 39.8 | 37.7 | 23.6 |
| Refrigerating capacity (kW) | 81 | 60.6 | 37.2 |
| Heating Load (kW) | 27 | 34.7 | 42.2 |
The carbon monodixe conversion multi-production process and device of the utility model design are ensureing the efficient conversion ratios of CO, meet life
While production. art requirement, it is possible to achieve generate electricity, freeze, heat supply output is supplied, system energy efficiency is high, and energy-saving effect is notable.
The principle that simply explanation the utility model described in above-described embodiment and specification is created, does not therefore limit
Protection domain of the present utility model, on the premise of the utility model creative spirit and scope is not departed from, this technology utility model
Various changes and modifications are also had, these changes and improvements are both fallen within the range of claimed the utility model.This practicality is new
Type is not directed to partly same as the prior art or can be realized using prior art.
Claims (7)
1. a kind of coal hydrogen manufacturing CO converts multi-joint-production apparatus, it is characterised in that：The device includes the first reacting furnace（3）, second reaction
Stove（5）With the 3rd reacting furnace（6）；
The output channel of crude synthesis gas and the first gas-liquid separator（1）It is connected, first gas-liquid separator（1）Gaseous phase outlet
By crude synthesis gas heater（2）With the first reacting furnace（3）Input be connected, first reacting furnace（3）Output end according to
It is secondary by crude synthesis gas heater（2）, the first waste heat boiler（4）With the second reacting furnace（5）Input be connected；
Second reacting furnace（5）Output end pass through the second waste heat boiler（7）With the 3rd reacting furnace（6）Input be connected,
3rd reacting furnace（6）Output end and the second gas-liquid separator（8）It is connected, second gas-liquid separator（8）Top
Output end passes through generator（9）With the 3rd gas-liquid separator（10）It is connected, the 3rd gas-liquid separator（10）The output at top
End passes through heating heater（11）With the 4th gas-liquid separator（12）It is connected, the 4th gas-liquid separator（12）The output at top
End is by conversion gas end cooler（13）With the 5th gas-liquid separator（14）It is connected, the 5th gas-liquid separator（14）Top it is defeated
Go out end to be connected with depickling unit.
2. coal hydrogen manufacturing CO according to claim 1 converts multi-joint-production apparatus, it is characterised in that：The first described waste heat boiler
（4）With first circulation working medium generating set（15）Matching is connected；The second described waste heat boiler（7）Generated electricity with second circulation working medium
Unit（16）Matching is connected；Described generator（9）With absorption type refrigeration circulation device（17）Matching is connected.
3. coal hydrogen manufacturing CO according to claim 2 converts multi-joint-production apparatus, it is characterised in that：Described first circulation working medium
Generating set, second circulation working medium generating set are that card Linne is circulated or Rankine cycle；Described absorption type refrigerating unit is heat
Drive kind of refrigeration cycle or heat/work(composite flooding kind of refrigeration cycle.
4. the coal hydrogen manufacturing CO according to Claims 2 or 3 converts multi-joint-production apparatus, it is characterised in that：Described absorption system
The cycle fluid that device for cooling is used is lithium bromide-water, ammoniacal liquor, R134a-DMF or ionic liquid-water.
5. coal hydrogen manufacturing CO according to claim 1 converts multi-joint-production apparatus, it is characterised in that：3rd reacting furnace（6）
Output end pass through the second waste heat boiler（7）With the second gas-liquid separator（8）It is connected.
6. coal hydrogen manufacturing CO according to claim 2 converts multi-joint-production apparatus, it is characterised in that：The second circulation working medium hair
The second waste heat boiler that group of motors is used is double heat source combined-type heat exchangers.
7. coal hydrogen manufacturing CO according to claim 1 converts multi-joint-production apparatus, it is characterised in that：First reacting furnace（3）, second
Reacting furnace（5）With the 3rd reacting furnace（6）It is axial-radial flow reactor, using insulation fix bed structure.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620312482.9U CN206266222U (en) | 2016-04-14 | 2016-04-14 | A kind of coal hydrogen manufacturing CO converts multi-joint-production apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620312482.9U CN206266222U (en) | 2016-04-14 | 2016-04-14 | A kind of coal hydrogen manufacturing CO converts multi-joint-production apparatus |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206266222U true CN206266222U (en) | 2017-06-20 |
Family
ID=59036803
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201620312482.9U Withdrawn - After Issue CN206266222U (en) | 2016-04-14 | 2016-04-14 | A kind of coal hydrogen manufacturing CO converts multi-joint-production apparatus |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN206266222U (en) |
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2016
- 2016-04-14 CN CN201620312482.9U patent/CN206266222U/en not_active Withdrawn - After Issue
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