CN1183380A - Flow dividing process for ammonia or alcohol synthesis reaction system - Google Patents
Flow dividing process for ammonia or alcohol synthesis reaction system Download PDFInfo
- Publication number
- CN1183380A CN1183380A CN96118424A CN96118424A CN1183380A CN 1183380 A CN1183380 A CN 1183380A CN 96118424 A CN96118424 A CN 96118424A CN 96118424 A CN96118424 A CN 96118424A CN 1183380 A CN1183380 A CN 1183380A
- Authority
- CN
- China
- Prior art keywords
- reactor
- gas
- ammonia
- pipe
- heat exchanger
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- 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
- Y02P20/50—Improvements relating to the production of bulk chemicals
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A split-flow process for synthesizing ammonia and methanol is disclosed. The hot gas from reactor goes through afterheat recovery unit, heat exchanger and water cooler into cooling and condense separation system. The ammonia separated is liquefied to obtain product. The circulated unreacted gas is splitted, one is 55-70% and goes through heat exchanger into reactor, and another is 30-45% and directly goes into reactor. Its advantages are less equipment, shorter pipeline, low flow resistance and high recovery of afterheat.
Description
A kind of ammonia alcohol synthesis reaction system flow dividing process that relates to is used for chemical industry ammonia, the synthetic production of methyl alcohol, belongs to chemical fertilizers production.
In the prior art, the ammonia of Chemical Manufacture and methyl alcohol are synthetic, are with in the unstripped gas input reactor, 230 ℃～500 ℃ of high temperature, carry out under high pressure 1～32MPa condition.Reactor is made up of high voltage bearing steel heavy wall urceolus and resistant to elevated temperatures stainless steel thin-wall inner core.Referring to Fig. 1, the concrete structure of reactor is mainly by inner core (01), urceolus (02), and cooler tube bundle (03), pipe core (04), interchanger (05), bottom four-way (06) constitutes.Bottom at pipe core (04) is separated into two sections with dividing plate (07), cooler tube bundle (03) is made of last endless tube (03A), following endless tube (03E), upcast (03B), cold pipe (03C), pipe connecting (03D), reactor in Fig. 1 is the product innovation that has several patents, but that the technical process outside reactor is still is traditional.
Be example explanation conventional process flow below with the ammonia synthesis reaction, referring to Fig. 1, from the unreacted circulation gas that cooling condensation separation system (012) is come out, its temperature is 30 ℃～45 ℃, enters, from top to bottom flows along annular space between inside and outside tube from reactor urceolus (02) top.Come out in an air outlet through the four-way (06) of reactor lower part, temperature reaches 60 ℃～80 ℃, enters heat exchanger (09), manage interior hot gas and be heated to 170 ℃～190 ℃.Through reactor lower part four-way (06) inlet mouth, enter for the second time between the pipe of bottom interchanger (05) of reactor inner core (01).From bottom to top entered the lower end of pipe core (04) after the hot gas heating in the pipe, through being attached thereto the upcast (03B) that connects, from bottom to top enter endless tube (03A), enter cooler tube bundle (03C) by last endless tube (03A), by the outer reaction heat gas heating of pipe, from top to bottom enter down endless tube (03D).Warp endless tube (03D) down arrives pipe core (04) with pipe connecting (03E), from bottom to top comes out from the upper end of pipe core (04).From top to bottom with internals in catalyst carry out building-up reactions.Its synthesising reacting heat is taken away by the unreacted cold air in the cooler tube bundle (03C).Through reacted hot gas, about 410 ℃～450 ℃ of its temperature, enter in interchanger (05) pipe of internals bottom, with the outer unreacted cold air of heating tube, reacted hot gas is come out by reactor lower part four-way (06) two, temperature is about 280 ℃～380 ℃ and enters waste-heat recoverer (08), and the soft water that heating tube is outer produces steam and supplies outward.The hot air temperature of coming out is reduced to about 200 ℃, enters in the pipe of heat exchanger (09) the outer unreacting gas of heating tube.The reaction gas temperature of coming out is reduced to 130 ℃～140 ℃, enters soft water heater (010), and the outer soft water of heating tube is for plant area's oiler feed.From the reaction gas that soft water heater (010) comes out, temperature is reduced to 70 ℃～80 ℃, enters water-cooled comb (011), is managed outer cold water spray, cools to about 35 ℃, enters cooling condensation separation system (012).Be cooled in system below 0 ℃, the ammonia condensing in the reactant gases becomes liquefied ammonia, isolates rice and is processed into product.The H that restock is new
2, N
2Gas, and pressurization become unreacted circulation gas, enter reactor, react by aforementioned technical process.
Above described be the conventional process flow of synthetic ammonia and methyl alcohol, be not difficult to find out that there is following shortcoming in it:
1, heat recovery rate is low, equipment is many, consumption of cooling-water is big, with synthetic ammonia is example, one goes out 60 ℃～70 ℃ of gas temperatures, two go out 280 ℃～320 ℃ of gas temperatures, two go out gas behind waste-heat recoverer (08), temperature is reduced to about 200 ℃, in heat exchanger (09), two go out gas and one goes out gas and carries out heat exchange, and its temperature variation is: two go out hot gas reduces to 110 ℃～130 ℃ from 180 ℃～200 ℃, and cold air is warming up to 170 ℃～190 ℃ from 60 ℃～70 ℃, and the cold junction heat transfer temperature difference is 50 ℃ therebetween.This moment hot air temperature up to 110 ℃～120 ℃ just enter water-cooled row and be cooled to 35 ℃, a large amount of reaction heat are not fully utilized, and must establish a soft water heater in the middle of therefore, utilize 110 ℃～120 ℃ hot gas heating soft water.But soft water can only be heated to 80 ℃～90 ℃, and for factory, this is low potential energy hot water, and purposes is little.
2, as soft water heater is not set, then the consumption of cooling-water at water-cooled comb (011) is bigger.
3, the 3rd shortcoming is, all gas all will pass through all equipment, long flow path, and resistance is big.
In view of this, purpose of the present invention just provides a kind of simplified equipment, and heat recuperation is effective, and the water consumption is few, and pipeline is short, and is easy to maintenance, the flow dividing process of rational synthetic ammonia of technical process and methyl alcohol.
The present invention adopts following technical proposals, and two advance one goes out shunt method, and reactor does not structurally change, the cancellation soft water heater, the circulation gas that the cooling condensation separation system is separated is before entering reactor, circulation gas is shunted, be divided into two strands; One about 55～70% circulation gas enter heat exchanger and are heated to 170 ℃～190 ℃ and enter reactor; Another strand is about 30～45%, and temperature is that 25 ℃～45 ℃ circulation gas directly enters the inside and outside tube of reactor annular space.Realize purpose of the present invention by such scheme,, in detail the feature of system architecture of the present invention and technical process is described in detail below in conjunction with drawings and Examples.
Fig. 1 is an original system structural manufacturing process schema
Fig. 2 is a structural manufacturing process schema of the present invention
Referring to Fig. 1～Fig. 2, in Fig. 2, reactor is made of inner core (1), urceolus (2), cooler tube bundle (3), pipe core (4), bottom interchanger (5), bottom side four-way (6), time endless tube (7), upcast (8), cold pipe (9), last endless tube (10), airway (11), waste-heat recoverer (12), heat exchanger (13), water-cooled row (14), cooling condensation separation system (15).
In Fig. 2, be two to advance one and go out shunt method, different with conventional process flow, from cooling condensation separation system (15) temperature of coming out is that 30 ℃～45 ℃ circulation gas is divided into two strands at the A point, is communicated with reactor with parallel way, and one accounts for the 55-70% that separates airshed, be transported between the pipe of heat exchanger (13), be heated to 170 ℃～190 ℃ by hot gas in the pipe,, arrive between the pipe of reactor lower part interchanger (5) through two inlet mouths of reactor bottom side four-way (6).From bottom to top, be heated to 350 ℃～380 ℃, enter pipe core (4) with the interior top-down thermal response gas heat exchange of pipe.Reach the top of pipe core (4) from bottom to top, turn back down with reactor bed in catalysis, carry out the ammonia synthesis thermopositive reaction, enter then in the pipe of interchanger (5), enter waste-heat recoverer (12) through bottom side four-way (6), heat exchanger (13), water-cooled row (14) arrives cooling condensation separation system (15) and finishes a circulation.
Another strand accounts for the 30-45% unreacted circulation gas of separating airshed, enters the inside and outside simple annular space of reactor from (6) one imports of reactor bottom side four-way.From bottom to top, arrive the inner core top cover, enter airway (11) by two inlet mouths on the top cover, the reaction gas temperature of this moment can reach 100 ℃～150 ℃.Unreacting gas from top to bottom, endless tube in the arrival (10), through cold pipe (9), following endless tube (7) passes to upcast (8).Its mouth of pipe flushes with pipe core (4) mouth of pipe or a little less than pipe core (4) mouth of pipe appropriate location.The unreacting gas that is come out by upcast (8) compiles to mix with gas top of chamber in reactor that pipe core (4) comes out and turns back down, from top to bottom carries out ammonia synthesis reaction by reactor under the bed catalysis.Reaction back gas temperature reaches 410 ℃～450 ℃.Enter in the pipe of bottom interchanger (5), be cooled to 300 ℃～380 ℃.Through waste-heat recoverer (12), the outer soft water of heating tube produces steam and supplies outward, hot gas is cooled to about 200 ℃, enter in heat exchanger (13) pipe, heating unreacted circulation gas, make the temperature of unreacted circulation gas bring up to 170 ℃～190 ℃, and the hot air temperature in the pipe is reduced to 70 ℃～90 ℃ by about 200 ℃ by 30 ℃～45 ℃.Enter water-cooled row (14) then, managed about outer cold water spraying cooling to 35 ℃, enter cooling condensation separation system (15); After the separation of ammonia, replenish H
2, N
2Gas, pressurization is carried out next one circulation by aforementioned technical process.
According to the above, the invention has the advantages that:
1, compares with traditional handicraft, saved a high pressure soft water heater, correspondingly shorten Length of pipeline, reduced the gas flow resistance.
2, in conventional process flow, though some reactor assembly is not provided with soft water heater, but the hot air temperature that enters water-cooled row (14) this moment up to 110 ℃～120 ℃, and technical process of the present invention, the temperature that enters water-cooled row only is 70 ℃～90 ℃, that is utilization of Heat of Reaction improves 40 ℃ of left and right sides temperature difference heats, and being used to heating steam, this part heat supplies outward, the steam that this part heat produces, bigger than 60 ℃～70 ℃ hot soft water use value of low temperature, the transmission heat waste is little.
3, the unreacted circulation gas of this technical process is that two strands of parallel forms enter reactor, is two to advance one and go out shunting.Compare with traditional technology, not every gas all will pass through all parts of reactor, and its resistance can reduce by 1/2～1/3, improved the security of reactor simultaneously, just in case there is a path to break down, another still can temporarily undertake the task of pipeline, and the unlikely circuit failure that causes is out of service.The present invention not only is used for ammonia synthesis, and is suitable equally for methyl alcohol and other similar reactors.
Claims (2)
1, a kind of ammonia alcohol synthesis reaction system flow dividing process that relates to is used for the synthetic production of chemical industry ammonia and methyl alcohol.It comprises reactor and outer heat exchanger and the cooling condensation separation system of reactor, it is characterized in that, two advance one goes out shunt method, by the synthetic hot gas that reflects of reactor warp, through waste-heat recoverer (12) heating soft water recovery waste heat, heat exchanger (13) heating unreacted circulation gas, water-cooled row (14) cooling hot gas heat release, enter liquefied ammoniaization or the thick methyl alcohol that cooling condensation separation system (15) separates and make product, separate unreacted circulation gas, after tonifying Qi pressurization, be divided into two strands and be connected with reactor with shunting mode in parallel.
2, ammonia according to claim 1, the alcohol synthesis reaction system flow dividing process, it is characterized in that, unreacted circulation gas is split into two strands from the A point, one accounts for airshed 55-70% temperature is that 30 ℃～45 ℃ gas enters in the reactor through two inlet mouths of heat exchanger (13) through reactor bottom side four-way (6), through between reactor lower part interchanger (5) pipe, ammonia synthesis reaction is carried out in the catalysis that enters in pipe core (4) top and the reactor bed, the 30-45% that another strand accounts for airshed enters annular space between inner core (1) and urceolus (2) from an inlet mouth of reactor bottom side four-way (6), through airway (11), last endless tube (10), cold pipe (9), following endless tube (7), upcast (8) compiles with the unreacting gas that pipe core (4) comes out and mixes, carry out ammonia synthesis reaction with the catalysis in the reactor bed, temperature of reaction can reach 410 ℃～450 ℃, in the pipe of interchanger (5), come out from reactor bottom side four-way (6), through waste-heat recoverer (12), heat exchanger (13), water-cooled row (14) arrives cooling condensation separation system (15) and finishes a circulation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96118424A CN1084297C (en) | 1996-11-22 | 1996-11-22 | Flow dividing process for ammonia or alcohol synthesis reaction system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96118424A CN1084297C (en) | 1996-11-22 | 1996-11-22 | Flow dividing process for ammonia or alcohol synthesis reaction system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1183380A true CN1183380A (en) | 1998-06-03 |
| CN1084297C CN1084297C (en) | 2002-05-08 |
Family
ID=5125083
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN96118424A Expired - Lifetime CN1084297C (en) | 1996-11-22 | 1996-11-22 | Flow dividing process for ammonia or alcohol synthesis reaction system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1084297C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102688734A (en) * | 2012-06-29 | 2012-09-26 | 石家庄工大化工设备有限公司 | Coal-made natural gas reactor |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1004443B (en) * | 1987-02-21 | 1989-06-07 | 贾培启 | Portable numerical universal thermometer |
| CN1031458C (en) * | 1993-07-24 | 1996-04-03 | 刘金成 | Waste heat recovery technology used in shift section of synthetic ammonia process |
| CN1039700C (en) * | 1995-12-05 | 1998-09-09 | 连云港化肥厂 | Producing method for synthetic ammonia |
-
1996
- 1996-11-22 CN CN96118424A patent/CN1084297C/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102688734A (en) * | 2012-06-29 | 2012-09-26 | 石家庄工大化工设备有限公司 | Coal-made natural gas reactor |
| CN102688734B (en) * | 2012-06-29 | 2014-03-12 | 石家庄工大化工设备有限公司 | Coal-made natural gas reactor |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1084297C (en) | 2002-05-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CA2612961C (en) | Compact reforming reactor | |
| US20070293590A1 (en) | Method for Carrying Out Heterogeneous Catalytic Exothermic Gas Phase Reactions | |
| CN102171170A (en) | Method and system for the production of methanol | |
| CN102850183B (en) | Methanol synthesis system and method | |
| WO2013097958A1 (en) | Adiabatic multi-bed catalytic converter with inter-bed cooling and a related process | |
| EP0256299B1 (en) | Ammonia synthesis converter | |
| US20070232801A1 (en) | High Pressure Method for Producing Pure Melamine in a Vertical Synthesis Reactor | |
| US6686398B1 (en) | Method and arrangement for producing methanol | |
| US4839391A (en) | Method and reactor for catalytic methanization of a gas containing CO, CO2 and H2 | |
| RU2005131948A (en) | REFORMING — INSTALLATION OF PARTIAL OXIDATION — REFORMING HEAT EXCHANGER DEVICE | |
| ZA200500276B (en) | Waste-heat boiler for claus plant | |
| CN101058534B (en) | Device and method for preparing dimethyl ether from methanol | |
| RU2074024C1 (en) | Method for exothermic heterogeneous synthesis and reactor for its embodiment | |
| JPS59169529A (en) | Catalytic gas synthesis method and device | |
| CN100386138C (en) | Process and equipment for internal heat exchanging catalytic reaction | |
| CN1084297C (en) | Flow dividing process for ammonia or alcohol synthesis reaction system | |
| CN205917020U (en) | A equipment for cooling off hydrogeneous forming gas | |
| WO2001012310A1 (en) | Catalyst tubes for endothermic reaction especially for the production of hydrogen and syngas | |
| CN115340095A (en) | Cold hydrogenation heat energy recovery system and method | |
| CN107032300B (en) | A kind of hydrogen production by methanol system that reactor feed temperature is stable | |
| CN212492844U (en) | Multi-section heat exchanger de-hydrocarbon comprehensive tower | |
| US3957449A (en) | Synthesis plant | |
| CN209702624U (en) | The parallel methanol synthesis reaction system of double-reactor | |
| US6482382B1 (en) | Process and converter for the preparation of ammonia | |
| CN2570725Y (en) | Column-pipe type heat exchanger for recovery of thermal energy in urea production |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: HUNAN ANCHUN HIGH AND NEW TECHNOLOGY CO., LTD. Free format text: FORMER OWNER: ANCHUN ENERGY-SAVING TECHNOLOGY CO., LTD., HUNAN PROV. Effective date: 20060303 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20060303 Address after: 410015 No. 135 Yuejin Road, Hunan, Changsha Patentee after: Hu'nan Anchun High & New Technology Co., Ltd. Address before: 410007 No. 135 Yuejin Road, Hunan, Changsha Patentee before: Anchun Energy-saving Technology Co., Ltd., Hunan Prov. |
|
| CX01 | Expiry of patent term |
Granted publication date: 20020508 |
|
| EXPY | Termination of patent right or utility model |