Classifications

• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
  • C10K1/00—Purifying combustible gases containing carbon monoxide
  • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
  • C10K1/00—Purifying combustible gases containing carbon monoxide
  • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
  • C10K1/06—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials combined with spraying with water
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
  • C10B43/00—Preventing or removing incrustations
  • C10B43/02—Removing incrustations
  • C10B43/08—Removing incrustations with liquids
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
  • C10B43/00—Preventing or removing incrustations
  • C10B43/14—Preventing incrustations

Definitions

• the invention relates to a method for flushing norkoolers of a coking plant according to the preamble of claim 1.
• the raw coke oven gas is first cooled in a direct raw gas cooling with the so-called Norlagen sprinkling water in a template.
• the raw coke oven gas is cooled to a temperature of approx. 80 ° C and at the same time part of the carried solids part is washed out of the raw coke oven gas and separated in the liquid phase together with the tar and condensate.
• the coke oven raw gas is cooled in an indirect cooling from approx. 80 ° C to approx. 20 ° C.
• a large part of the naphthalene contained in the raw coke oven gas sublimes.
• tar-like, solids-containing ingredients of the coke oven raw gas are separated on the outer walls of the cooling tubes of the precoolers. In conjunction with the sublimed naphthalene, there is a risk that the precooler will become blocked after a relatively short operating time.
• the condensate separated in the pre-coolers and the naphthalene-containing rinsing tar cannot be conveyed directly to the tar separation at a temperature of approx. 20 ° C, since otherwise the emulsion would form and the tar separation would no longer work.
• the precooler condensates with the naphthalene-containing flushing tar are therefore usually pumped back to the individual raw gas feeds of the coke oven batteries and mixed there with the hot condensed liquid phase coming from the coke oven.
• the temperature of the recirculated pre-cooler condensate, including the rinsing tar raised to approx. 80 ° C, but mixing takes place at the same time with the tar coming from the coke oven, so that ultimately only one tar enriched with naphthalene reaches and separates from the tar Rinsing the precooler is available.
• the unpublished DE 100 51 349 AI discloses a process for the extraction of naphthalene from raw coke oven gas, in which the raw coke oven gas is cooled and the naphthalene contained in the raw coke oven gas is obtained directly.
• the unpublished DE 100 07 503 AI discloses a process for the treatment of raw coke oven gas, in which the raw coke oven gas after cooling is passed through an electrostatic filter and then into the precooler, the outlet of the electric feeder being used for purging in the precoolers.
• DE 26 52 499 AI discloses a method for cooling the raw coke oven gas, in which the precooler is divided into two stages, with no precooler purging being carried out in the first stage and sprinkling of the gas with the recycle in the second stage the precooler condensate is made.
• DE 36 14 851 AI discloses a method for rinsing precoolers of a coking plant, in which the precoolers are rinsed with the liquid phase obtained from the template.
• lighter components BTX aromatics
• the invention has for its object to provide a method in which a blockage of the precooler by naphthalene deposits is reliably avoided and thus a high availability of the precooler is guaranteed and in which additional cleaning methods are unnecessary. This object is achieved by the features of patent claim 1.
• the method according to the invention is based on the basic idea of using the liquid phase obtained in the case of direct raw gas cooling in the raw gas receiver, which contains a relatively low naphthalene tar, for purging the precooler.
• the liquid phase of at least one raw gas receiver is not mixed with the precooler condensates which contain the flushing tar which has already been enriched with naphthalene and is collected in a separate tar separator.
• This separately collected liquid phase contains the particularly low naphthalene tar.
• the existing tar separator can be used as a separate tar separator. This has the advantage that no additional tar separator and thus additional investments are required.
• this low-naphthalene liquid phase is used for flushing the cooler tubes in the pre-coolers.
• the water portion of the separately collected liquid phase can be separated in the separate tar separator.
• the low naphthalene tar can also be mixed with water for use as a flushing tar.
• the tar or the liquid phase can be freed from the solids in a tar centrifuge. This procedure ensures that no solids get into the precooler through the tar or the liquid phase.
• the naphthalene of the coke oven raw gas sublimates when it cools from approx. 80 ° C to approx. 20 ° C and is deposited on the cooling pipes of the precooler. It is now possible to prevent the precooler from becoming blocked by continuously flushing it with the low-naphthalene tar with the liquid phase previously obtained from at least one raw gas receiver which is not charged with precooler condensates.
• Rinsing with low-naphthalene tar can in principle be carried out with all suitable nozzles, preferably in the upper area of the pre-cooler. Since the tar is low in naphthalene, placing the tar in the pre-cooler at one point is sufficient for washing success.
• the rinsing should take place in three levels, above, in the middle and below. This ensures in any case that deposits do not form on the cooler pipes.
• Flushing in the pre-coolers with a baffle ring nozzle known per se is preferred.
• the impact ring nozzles ensure optimal distribution of the low-naphthalene tar on the pipes and the inner walls of the precooler.
• the tarry and aqueous condensates that run off at the foot of the precooler are conveyed as usual to the remaining raw gas feeds, where they are processed together with the liquid phase that results from direct raw gas cooling.
• Continuous pre-cooler operation can be maintained by the method according to the invention, since deposits do not form on the cooler tubes and the additional cleaning processes are no longer necessary.
• the emissions that occur during the additional cleaning processes are also avoided. Flushing with low-naphthalene tar significantly increases the availability of pre-cooling.
• the investment costs are reduced because fewer pre-coolers have to be provided. Since the cleaning processes can be omitted, the personnel and material costs are also reduced.
• Continuous pre-cooler operation ensures that constant low coke oven raw gas temperatures are maintained at the pre-cooler outlet.
• the coke oven gas quality improves because the hydrogen sulfide, ammonia and benzene leaching can be carried out more effectively at a constant low temperature. Corrosion does not occur in the production of benzene, since the condensates containing hydrogen sulfide and ammonia are avoided.
• Figure 1 is a process diagram of the method for rinsing the precooler with the low naphthalene tar.
• the treatment of the raw coke oven gas is shown schematically in FIG.
• the raw coke oven gas coming from the coke ovens 1 is cooled in templates 2 and 2a with the help of sprinkling water 14 directly to approximately 80 ° C. and passed into the precooler 3.
• the raw coke oven gas is conveyed into a coke oven gas cleaning system 4 before it reaches a consumer 5.
• the condensates running out of the pre-coolers 3 with the naphthalene-rich flushing tar are required via a line 13 to the template 2, where heating and mixing with the tar obtained in the case of direct raw gas cooling takes place.
• This liquid phase from the template 2 is fed via a line 9 into a tar separator 6 for separating the tar from the coal water.
• the coal water is conveyed via line 7 for further processing.
• the separated naphthalene-rich tar is transported via line 8 for loading.
• the liquid phase from the template 2a is passed via a line 10 into a separate tar separator 11 and separated into coal water and low-naphthalene tar.
• the low-naphthalene tar is conveyed via a line 12 to the precoolers 3 and is used there to rinse the cooling pipes.

Landscapes

• Chemical & Material Sciences (AREA)
• Engineering & Computer Science (AREA)
• Combustion & Propulsion (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• Organic Chemistry (AREA)
• Chemical Kinetics & Catalysis (AREA)
• General Chemical & Material Sciences (AREA)
• Materials Engineering (AREA)
• Industrial Gases (AREA)
• Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
• Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
• Separation By Low-Temperature Treatments (AREA)

Applications Claiming Priority (3)

Publications (2)

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ID=7694927

Family Applications (1)

Country Status (9)

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• 2001
  • 2001-08-15 DE DE10139172A patent/DE10139172C1/de not_active Expired - Fee Related
• 2002
  • 2002-07-24 TW TW091116448A patent/TW555844B/zh not_active IP Right Cessation
  • 2002-08-10 WO PCT/EP2002/008978 patent/WO2003016437A2/fr not_active Ceased
  • 2002-08-10 AU AU2002329241A patent/AU2002329241A1/en not_active Abandoned
  • 2002-08-10 AT AT02764842T patent/ATE328985T1/de active
  • 2002-08-10 KR KR10-2004-7001543A patent/KR20040025935A/ko not_active Withdrawn
  • 2002-08-10 EP EP02764842A patent/EP1419221B1/fr not_active Expired - Lifetime
  • 2002-08-10 DE DE50207122T patent/DE50207122D1/de not_active Expired - Lifetime
  • 2002-08-10 CN CNA028160657A patent/CN1543497A/zh active Pending
• 2004
  • 2004-01-29 ZA ZA200400726A patent/ZA200400726B/xx unknown

Non-Patent Citations (1)

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