AU603155B2 - Process for the synthesis of ammonia - Google Patents

Process for the synthesis of ammonia Download PDF

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Publication number
AU603155B2
AU603155B2 AU81470/87A AU8147087A AU603155B2 AU 603155 B2 AU603155 B2 AU 603155B2 AU 81470/87 A AU81470/87 A AU 81470/87A AU 8147087 A AU8147087 A AU 8147087A AU 603155 B2 AU603155 B2 AU 603155B2
Authority
AU
Australia
Prior art keywords
converter
gas
ammonia
cooling
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.)
Ceased
Application number
AU81470/87A
Other versions
AU8147087A (en
Inventor
Heinz Graeve
Hans-Joachim Herbort
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
ThyssenKrupp Industrial Solutions AG
Original Assignee
Uhde GmbH
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Uhde GmbH filed Critical Uhde GmbH
Publication of AU8147087A publication Critical patent/AU8147087A/en
Application granted granted Critical
Publication of AU603155B2 publication Critical patent/AU603155B2/en
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/02—Preparation, purification or separation of ammonia
    • C01C1/04—Preparation of ammonia by synthesis in the gas phase
    • C01C1/0405—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst
    • C01C1/0417—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst characterised by the synthesis reactor, e.g. arrangement of catalyst beds and heat exchangers in the reactor
    • C01C1/0423—Cold wall reactors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0285—Heating or cooling the reactor
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/02—Preparation, purification or separation of ammonia
    • C01C1/04—Preparation of ammonia by synthesis in the gas phase
    • C01C1/0405—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/02—Preparation, purification or separation of ammonia
    • C01C1/04—Preparation of ammonia by synthesis in the gas phase
    • C01C1/0405—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst
    • C01C1/0447—Apparatus other than synthesis reactors
    • C01C1/0452—Heat exchangers
    • 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
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
  • Silicon Compounds (AREA)
  • Catalysts (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Detergent Compositions (AREA)
  • Diaphragms For Electromechanical Transducers (AREA)
  • Measurement Of Radiation (AREA)
  • Industrial Gases (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

Starting from a synthesis process for ammonia in which converter parts heated in the process by the hot gas are cooled by colder gas, a solution is provided which in particular makes possible thinner-walled components and/or less expensive material for the converters and other components. According to the process, this is achieved by repeatedly recirculating the process gas over the ammonia converter(s), separating the ammonia at the end of a cooling space as condensate and passing the fresh gas as cooling gas in the area of hot process gases without contacting the latter. The device having at least one converter and one heat exchanger is distinguished in that a second converter (3) is additionally provided essentially in a parallel arrangement to the first converter (2) with an intermediate steam generator (4) as a heat exchanger in the floor area of both converters (2, 3), a fresh gas supply being arranged as a cooling gas supply in an antechamber (12) of the heat exchanger (4) and a twin pipe connection (11) to the first converter being provided for rinsing a hot gas pipe (9) coming from the first converter (2). <IMAGE>

Description

-~IIYI~-Y-I- i IIC- II.. 1 ~155
AUSTRALIA
PATENTS ACT 1952 COMPLETE SPECIFICATION
(ORIGINAL)
FOR OFFICE USE Application Number: Lodged: Complete Specification Lodged: Accepted: Published: This document contains the anildments made under Section 49 and is correct for printhig.
t 0O 'Es.
'a a -a Priority: Related Art: TO BE COMPLETED BY APPLICANT Name of Applicant: Address of Applicant: Actual Inventor: UHDE GMBH Friedrich-Uhde-Str. 4600 Dortmund 1 FEDERAL REPUBLIC OF GERMANY Hans-Joachim HERBORT and Heinz GRAEVE ARTHUR S. CAVE CO.
Patent Trade Mark Attorneys Goldfields House 1 Alfred Street SYDNEY N.S.W. 2000
AUSTRALIA
the invention entitled PROCESS FOR Address for Service: *0 a asr Complete Specification for THE SYNTHESIS OF AMMONIA.
The following including the statement is a full description of this invention best method of performing it known to me:- 1 ASC 49 2 .The invention relates to a process for the synthesis of ammonia in which hot-gas-bearing converter elements are cooled by means of a cooler gas.
It is known to cool the outlet nozzles through which the hot gas leaves a converter, by means of cooler gases. In the procedures known, cooler process gas is used for cooling, i.e. a gas with a comparatively high ammonia content. This already serves to mitigate the stress on these structural elements; however, a high-grade steel still must be used in 0* their construction. Such a cooling method in which the entire 0quantity of cooler process gas leaving a heat exchanger is introduced into the ammonia converter is described inthe European Application 83 307 204. A consequence of the solution described in this application is, among others, that depending upon the heat exchange taking place in the heat exchanger, the cooler process gas used for cooling in fact has a relatively high temperature, which requires appropriate steel grades to be used for the structural elements in contact "iith the hot gases.
The present invention seeks to provide a solution i this problem, which allows, above all, structural elements of smaller wall thickness and/or less expensive materials to be used for the converter, in particular for the outlet nozzles.
In the procedure according to this invention, the process gas is subjected to a multiple recycle flow throught-said converter elements; the amonia is separated from and drawn off from the recycle flow at an end of a cooling section, and that feed gas is used to cool structural elements ducting hot process gas effluent emerging from a catalyst bed.
L.!
-3- For this procedure a comparatively cool feed gas, e.g.
gas at a temperature of 30°C, is used to cool hot process gas areas. This allows the use of a lower than normal design temperature, since the usual temperature of about 400 0 C is lowered by approximately 150 0 C. This permits the use of structural elements of smaller wall thickness and, in particular, of construction materials which are less expensive. Since the feed gas is effectively free of NHK nitration due to NH, ceases to be a problem, which is also a reason why less expensive materials can be used.
An embodiment of the invention provides for the cooling feed cas being introduced in the transition zone between a steam gererator and an ammonia converter and being directed through a space in the double wall for coolinc the converter oo and, i- necessary, for cooling further plant sections.
It is pointed out once more that the feed gas used for cooling is a gas practicallv free of NH 3 The advantages involved are beneficial to the other process steps, too.
A special preferred embodiment of the invention provides for the cooling feed gas being routed in such a way that its maximum temperature change is limited to 70 0 C, the gas being heated generally about 20 to 40 0
C.
The invention may also be applied advantageously for processes with at least two separate ammonia converters. In such a process design, this invention provides for the cooling feed gas leaving the channel of a steam generator to be used for ALI0 ooling the shell of a first and, thereafter, of a second t It 1 t l -4converter before being reintroduced into the synthesis loop, if required.
In a preferred embodiment the parameters of the feed gas used for cooling are: NH 3 content less than 0.2% by volume, inlet temperature 20 to 150°C, make-up quantity 10 to 40% of the recycle quantity.
The technique described above for a device with at least one converter and one heat exchanger is applicable when a second converter is arranged in parallel with the first converter and when an intermediate steam generator as heat exchanger is provided in the base area of both converters. In this case, too, a heat exchancer channel is ecui;ped wiz- an intake nozzle for the cooling feed gas as well as wi-h a double oipe for circulating the hot gas leaving the first converter.
S According to the state of the art as described in the European Application 83 307 204, the principle of :he supply of a cooler gas leaving the channel of a heat exchanger and intended. for shell cooling is well known. However, according to this invention besides the installation of two converters in a closed process, the present invention also provides for the supply of cool feed gas as cooling agent. This offers the particular advantage, besides those already described above, that it is quite unexpectedly not necessary to recycle the total cooling gas quantity. The present invention requires only a fraction of the cooling gas to be recycled since only the A.LLU portion of the recycle gas corresponding mainly to the ndensate withdrawn from the process has to be replaced by
I
5 fresh feed gas.
A further embodiment of the invention provides for the first and second converter being equipped with a double wall provided with a cooling-gas-charged annular slot, and at least the second converter being equipped with a double pipe for discharging both the process gas and the cooling gas.
It may be expedient, as also provided for by this invention, if the double pipe of the first converter and/or the double pipe of the second converter are installed eccentrically in the converter bottom.
A compact design can be obtained by admitting a S flow from the double pipe of the second converter to the channel of another heat exchancer or steam generator.
If the aforesaid design has been chosen, it may o i additionally be suitable to acccmodate the first and second heat exchanger in a common housing and to choose a U-shaped arrangement tocether with the arnonia converters.
The invention may be described in more detail as follows, with particular reference to the attached drawings in which: Fiaure 1 reoresents a ceneral view of a device as per the invention.
Figure 2 represents an enlarged sectional view according to the line II-II as marked in Figure 1.
Figure 1 shows a simplified representation of the device 1 which consists of a first converter 2 and a second ©converter 3, both in a vertical position, and of an intermediate 0a
I
-r I l( -6i t 1 f; horizontal steam generator unit 4. Above the steam generator 4 a drum may be located which, however, is not represented in Figures 1 and 2.
The special design of the device 1 shown in Figures 1 and 2 comprises, besides the steam generator 4, a further steam generator or heat exchanger 5 which, as a separate structural element, is arranged in parallel with the first heat exchanger 4.
An essential feature of the oresent invention is to use the feed gas for cooling the system. The position of the intake nozzle 6 is shown in Figure 1: further details of zhis nozzle may be seen from Ficure 2.
-n Figure 2 it can be seen tnha in the converters 2 and 3, the major wall sections have been desicned as a double wall structure, viz. double wall 7 with annular slot 3 for converter 2 and double wall 7' with annular slot 8' for converter 3. The hot process gas leaves the converter 2 through line 9 which, via a lateral outlet in the bottom 10 of the Sconverter 2, leads to the steam generator 4. This hcz line 9 has been designed as double pipe 11, the inner pipe being charged with hot process gas and the outer pipe being cooled by feed gas entering via nozzle 6 and flowing through channel 12 of the heat exchanger 4 into the annular slot 13. The gas passes from this annular slot 13 into the base 10 of the converter 2, and passes from there into the annular slot 8 in the wall 7 of converter 2.
The cooling gas then leaves the converter 2 and enters S he second converter 3 via line 14 represented by dash-dots in 1 7 Figure 1, flows through the annular slot 8' in the double wall 7' and leaves the converter 3 via annular slot 15 in the double pipe 16. In the example shown in Figure 2 the feed gas used for cooling theH passes through channel 17 of a further steam generator 5 and leaves the steam generator via nozzle 18.
As shown in Figure 2, the hot process gas first passes through the steam generator 4 and then enters the second converter 3 via a double pipe 11' which is arranged eccentrically
S*
like the double oiDe 11 of the first converter. This double pipe 11' may also be charged with cooling gas. Thereafter, the cooling gas may be withdrawn from the second channel 12' of the steam cenerator 4 for beina combined with the cher cocling gas.
This, however, is not shown in zhe Figures.
The embodiment of the invention described before by .g way of example permits, of course, a plurality of modifications without departin from the basic idea of the invenzion. Thus, it is also feasible to accommodate the steam generators 4 and in a common housing provided with the appropriate channels as well as hot gas intake and discharge lines etc.
p

Claims (10)

  1. 2. A process according to claim i, wherein said cooler gas is introduced in a transition zone between a steam generator and an ammonia converter and is directed through a space in a double wall for cooling said converter. e 3. A process according to claim 2, wherein said cooler gas is routed in such a way that its temperature change is limited to OOOO
  2. 4. A process according to claim 2, wherein said cooler gas CS temperature change is from 20°C to A process according to claim i, wherein the system includes at least two separate ammonia converters; the feed gas leaving a channel of a steam generator is used for cooling the shell of a first and, thereafter, of a second converter before being reintroduced into the synthesis loop, if required.
  3. 6. A process according to claim i, wherein the parameters of PI" '01" the feed gas used for cooling are as follows: NH 3 content less than 0.2% by volume, inlet temperature to 150"C, make-up quantity 10 to 40% of the recycle quantity.
  4. 7. A device for the synthesis of ammonia by performing a process according to any one of the preceding claims, having at ALI Co AMD/0260a 9 least one converter and at least one heat exchanger, wherein, the first converter is equipped with a double wall including a cooling gas charged annular slot, and a channel of the first heat exchanger is equipped with an intake nozzle for the cooling feed gas, as well as with a double pipe for circumcirculating the hot gas pipe leaving the first converter.
  5. 8. An apparatus for the synthesis of ammonia as claimed in claim 7 having at least two converters and at least one heat exchangev, wherein the second converter is arranged in parallel with the first converter and equipped with an intermediate steam generator as a first heat exchanger in the base area of both converters.
  6. 9. An apparatus according to claim 8, wherein the first and second converters are equipped with a double wall including a cooling-gas-charged annular slot, and at least the second converter is equipped with a double pipe for discharging both the process gas and the cooling gas. An apparatus according to claim 9, wherein the double pipe of the first converter and/or the double pipe of the second converter are installed eccentrically in the bottom of the converter.
  7. 11. An apparatus according to claim 9, wherein a flow from the double pipe of the second converter is admitted to the channel of a second heat exchanger or steam generator.
  8. 12. An apparatus according to claim 8, wherein the first heat exchanger and the second heat exchanger are accommodated in a common housing forming a U-shaped arrangement together with the ammonia conve ters. AMD/0260a 1
  9. 13. A process for the synthesis 7)f ammonia, substantially as hereindescribed.
  10. 14. An apparatus for the synthesis of ammonia, substantially as hereindescribed with reference to the accompanying drawings. DATED this 7th day of August, 1990. UHDE GMBH By Its Patent Attorneys ARTHUR S. CAVE CO. s 0
AU81470/87A 1986-11-28 1987-11-20 Process for the synthesis of ammonia Ceased AU603155B2 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19863640823 DE3640823A1 (en) 1986-11-28 1986-11-28 METHOD FOR THE SYNTHESIS OF AMMONIA
DE3640823 1986-11-28

Publications (2)

Publication Number Publication Date
AU8147087A AU8147087A (en) 1988-06-02
AU603155B2 true AU603155B2 (en) 1990-11-08

Family

ID=6315087

Family Applications (1)

Application Number Title Priority Date Filing Date
AU81470/87A Ceased AU603155B2 (en) 1986-11-28 1987-11-20 Process for the synthesis of ammonia

Country Status (11)

Country Link
EP (1) EP0268808B1 (en)
JP (1) JPS63144113A (en)
CN (1) CN87108053A (en)
AT (1) ATE83221T1 (en)
AU (1) AU603155B2 (en)
DE (2) DE3640823A1 (en)
DK (1) DK552287A (en)
ES (1) ES2035841T3 (en)
FI (1) FI83071C (en)
NO (1) NO874578L (en)
ZA (1) ZA878298B (en)

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4907643A (en) * 1989-03-22 1990-03-13 C F Braun Inc. Combined heat exchanger system such as for ammonia synthesis reactor effluent
US5236671A (en) * 1990-09-24 1993-08-17 C. F. Braun, Inc. Apparatus for ammonia synthesis
US7867465B2 (en) * 2008-05-29 2011-01-11 Kellogg Brown & Root Llc Cold wall horizontal ammonia converter
CN101551098B (en) * 2009-05-07 2011-09-21 中石油东北炼化工程有限公司吉林设计院 Steam generator in synthetic ammonia plant and control system thereof
US8043574B1 (en) * 2011-04-12 2011-10-25 Midwest Refrigerants, Llc Apparatus for the synthesis of anhydrous hydrogen halide and anhydrous carbon dioxide

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0113524A1 (en) * 1982-11-26 1984-07-18 Santa Fe Braun Inc. Ammonia converter
AU5698986A (en) * 1985-04-08 1986-11-05 Santa Fe Braun Inc. Temperature controlled ammonia synthesis process

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3721532A (en) * 1971-02-08 1973-03-20 Braun Co C Ammonia synthesis system
PL83843B1 (en) * 1972-05-10 1976-02-28 Instytut Nawozow Sztucznychpo
NL7306515A (en) * 1972-05-15 1973-11-19 Montedison Spa

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0113524A1 (en) * 1982-11-26 1984-07-18 Santa Fe Braun Inc. Ammonia converter
AU5698986A (en) * 1985-04-08 1986-11-05 Santa Fe Braun Inc. Temperature controlled ammonia synthesis process

Also Published As

Publication number Publication date
EP0268808B1 (en) 1992-12-09
FI83071B (en) 1991-02-15
FI874770A0 (en) 1987-10-29
JPS63144113A (en) 1988-06-16
DE3640823A1 (en) 1988-06-09
NO874578L (en) 1988-05-30
ZA878298B (en) 1988-05-03
DK552287D0 (en) 1987-10-21
AU8147087A (en) 1988-06-02
DE3783017D1 (en) 1993-01-21
FI874770A (en) 1988-05-29
DK552287A (en) 1988-05-29
FI83071C (en) 1991-05-27
CN87108053A (en) 1988-06-29
ES2035841T3 (en) 1993-05-01
ATE83221T1 (en) 1992-12-15
NO874578D0 (en) 1987-11-03
EP0268808A1 (en) 1988-06-01

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